# Patent

## Title
High vinyl terminated propylene based oligomers

## Abstract

This invention relates to a co-oligomer having an Mn of 300 to 30,000 g/mol comprising 10 to 90 mol % propylene and 10 to 90 mol % of ethylene, wherein the oligomer has at least X % allyl chain ends, where: 1) X=(−0.94(mole % ethylene incorporated)+100), when 10 to 60 mole % ethylene is present in the co-oligomer, and 2) X=45, when greater than 60 and less than 70 mole % ethylene is present in the co-oligomer, and 3) X=(1.83*(mole % ethylene incorporated)−83), when 70 to 90 mole % ethylene is present in the co-oligomer. This invention also relates to a homo-oligomer, comprising propylene, wherein the oligomer has: at least 93% allyl chain ends, an Mn of about 500 to about 20,000 g/mol, an isobutyl chain end to allylic vinyl group ratio of 0.8:1 to 1.2:1.0, and less than 100 ppm aluminum. This invention also relates to a process of making homo-oligomer, comprising propylene, wherein the productivity is greater than 4500 g/mmol Hf (or Zr)/hour.

## Background
CROSS-REFERENCE TO RELATED APPLICATIONS
This application is a divisional of U.S. Pat. No. 8,372,930, issued Feb. 12, 2013.


FIELD OF THE INVENTION
This invention relates to olefin oligomerization, particularly propylene-ethylene oligomerization, to produce vinyl terminated oligomers.
BACKGROUND OF THE INVENTION
Alpha-olefins, especially those containing about 6 to about 20 carbon atoms, have been used as intermediates in the manufacture of detergents or other types of commercial products. Such alpha-olefins have also been used as monomers, especially in linear low density polyethylene. Commercially produced alpha-olefins are typically made by oligomerizing ethylene. Longer chain alpha-olefins, such as vinyl-terminated polyethylenes are also known and can be useful as building blocks following functionalization or as macromonomers.
Allyl terminated low molecular weight solids and liquids of ethylene or propylene have also been produced, typically for use as branches in polymerization reactions. See, for example, Rulhoff, Sascha and Kaminsky, (“Synthesis and Characterization of Defined Branched Poly(propylene)s with Different Microstructures by Copolymerization of Propylene and Linear Ethylene Oligomers (Cn=26-28) with Metallocenes/MAO Catalysts,” Macromolecules 16 2006, 1450-1460), and Kaneyoshi, Hiromu et al. (“Synthesis of Block and Graft Copolymers with Linear Polyethylene Segments by Combination of Degenerative Transfer Coordination Polymerization and Atom Transfer Radical Polymerization,” Macromolecules 38 2005, 5425-5435).
Further, U.S. Pat. No. 4,814,540 discloses bis(pentamethyl cyclopentadienyl)hafnium dichloride, bis(pentamethyl cyclopentadienyl) zirconium dichloride and bis(tetramethyl n-butyl cyclopentadienyl)hafnium dichloride with methylalumoxane in toluene or hexane with or without hydrogen to make allylic vinyl terminated propylene homo-oligomers having a low degree of polymerization of 2-10. These oligomers do not have high Mn's and have at least 93% allylic vinyl unsaturation. Likewise, these oligomers lack comonomer and are produced at low productivities with a large excess of alumoxane (molar ratio≧600 Al/M; M=Zr, Hf). Additionally, no less than 60 wt % solvent (solvent+propylene basis) is present in all of the examples.
Teuben et al. (J. Mol. Catal. 62 1990, 277-87) used [Cp*2MMe(THT)]+[BPh4], M=Zr and Hf) to make propylene oligomers. For M=Zr a broad product distribution with oligomers up to C24 (Mn 336) was obtained at room temperature. Whereas for M=Hf only the dimer 4-methyl-1-pentene and the trimer 4,6-dimethyl-1-heptene were formed. The dominant termination mechanism appeared to be beta-methyl transfer from the growing chain back to the metal center, as was demonstrated by deuterium labeling studies.
X. Yang, et al. (Angew. Chem. Intl Edn. Engl. 31 1992 1375) discloses amorphous, low molecular weight polypropylene made at low temperatures where the reactions showed low activity and product having 90% allylic vinyls, relative to all unsaturations, by 1H NMR. Thereafter, Resconi, et al. (J. Am. Chem. Soc. 114 1992, 1025-1032), disclose the use of bis(pentamethylcyclopentadienyl) zirconium and bis(pentamethylcyclopentadienyl)hafnium centers to polymerize propylene and obtained beta-methyl termination resulting in oligomers and low molecular weight polymers with “mainly allyl- and iso-butyl-terminated” chains. As is the case in U.S. Pat. No. 4,814,540, the oligomers produced do not have at least 93% allyl chain ends, an Mn of about 500 to about 20,000 g/mol (as measured by 1H NMR), and the catalyst has low productivity (1-12,620 g/mmol metallocene.hr;>3000 wppm Al in products).
Similarly, Small and Brookhart, (Macromol. 32 1999, 2322) discloses the use of a pyridylbis amido iron catalyst in a low temperature polymerization to produce low molecular weight amorphous propylene materials apparently having predominant or exclusive 2,1 chain growth, chain termination via beta-hydride elimination, and high amounts of vinyl end groups. Dekmezian et al. (Macromol. 33, 2000, 8541-8548) discloses materials with up to about 81 percent vinyl termination made using dimethylsilyl bis(2-methyl, 4-phenyl-indenyl) hafnium dichloride and methylalumoxane in toluene at about 120° C. The materials have a number average molecular weight of about 12,300 (measured with 1H NMR) and a melting point of about 143° C.
Moscardi et al. (Organomet. 20, 2001, 1918) discloses the use of rac-dimethylsilylmethylene bis(3-t-butyl indenyl) zirconium dichloride with methylalumoxane in batch polymerizations of propylene to produce materials where “ . . . allyl end group always prevails over any other end groups, at any [propene].” In these reactions, morphology control was limited and approximately 60% of the chain ends are allylic.
Coates et al. (Macromol 2005 38, 6259) discloses preparation of low molecular weight syndiotactic polypropylene ([rrrr]=0.46-0.93) with about 100% allyl end groups using bis(phenoxyimine)titanium dichloride ((PHI)2TiCl2) activated with modified methyl alumoxane (MMAO; Al/Ti molar ratio=200) in batch polymerizations run between −20 and +20° C. for four hours. For these polymerizations, propylene was dissolved in toluene to create a 1.65 M toluene solution. Catalyst productivity was very low (0.95 to 1.14 g/mmol Ti/hr).
JP-2005-336092-A2 discloses the manufacture of vinyl-terminated propylene polymers using materials such as H2SO4 treated montmorillonite, triethylaluminum, triisopropyl aluminum, where the liquid propylene is fed into a catalyst slurry in toluene. This process produces substantially isotactic macromonomers not having a significant amount of amorphous material.
Rose et al (Macromolecules 2008, 41, 559-567) discloses poly(ethylene-co-propylene) macromonomers not having significant amounts of iso-butyl chain ends. Those were made with bis(phenoxyimine) titanium dichloride ((PHI)2TiCl2) activated with modified methylalumoxane (MMAO; Al/Ti molar ratio range 150 to 292) in semi-batch polymerizations (30 psi propylene added to toluene at 0° C. for 30 min, followed by ethylene gas flow at 32 psi of over-pressure at about 0° C. for polymerization times of 2.3 to 4 hours to produce E-P copolymer having an Mn of about 4800 to 23,300. In four reported copolymerizations, allylic chain ends decreased with increasing ethylene incorporation roughly according to the equation:

% allylic chain ends (of total unsaturations)=−0.95(mole % ethylene incorporated)+100.

For example, 65% allyl (compared to total unsaturation) was reported for E-P copolymer containing 29 mole % ethylene. This is the highest allyl population achieved. For 64 mole % incorporated ethylene, only 42% of the unsaturations are allylic. Productivity of these polymerizations ranged from 0.78×102 g/mmol Ti/hr to 4.62×102 g/mmol Ti/hr.

Prior to this work, Zhu et al. reported only low ( ̃38%) vinyl terminated ethylene-propylene copolymer made with the constrained geometry metallocene catalyst [C5Me4(SiMe2N-tert-butyl)TiMe2 activated with B(C6F5)3 and MMAO (Macromol 2002 35, 10062-10070 and Macromol Rap. Commun. 2003 24 311-315).
Janiak and Blank summarize a variety of work related to oligomerization of olefins (Macromol. Symp. 236 2006, 14-22).
In all the prior art no catalysts are shown to produce high allylic chain unsaturations in high yields, a wide range of molecular weight, and with high productivity for propylene-based polymerizations, especially propylene-ethylene copolymerizations. Thus, there is still a need for propylene based macromonomers that have allyl termination present in high amounts (90% or more), with control over a wide range of molecular weights that can be made at commercial temperatures (e.g. 25° C. and above) and commercial rates (5,000 g/mmol/hr productivity or more). Alternately, there is a need for propylene ethylene oligomers having structural robustness (where addition of ethylene raises viscosity and the solubility parameter—relative to propylene—and provides for potential crystallizable ethylene runs, while lowering glass transition temperature). Further, there is a need for propylene based reactive materials having vinyl termination which can be functionalized and used in additive applications.
SUMMARY OF THE INVENTION
This invention relates to a propylene co-oligomer having an Mn of 300 to 30,000 g/mol (as measured by 1H NMR) comprising 10 to 90 mol % propylene and 10 to 90 mol % of ethylene, wherein the oligomer has at least X % allyl chain ends (relative to total unsaturations), where: 1) X=(−0.94*(mole % ethylene incorporated)+100), when 10 to 60 mole % ethylene is present in the co-oligomer, and 2) X=45, when greater than 60 and less than 70 mole % ethylene is present in the co-oligomer, and 3) X=(1.83*(mole % ethylene incorporated)−83), when 70 to 90 mole % ethylene is present in the co-oligomer.
This invention further relates to a propylene oligomer, comprising more than 90 mol % propylene and less than 10 mol % ethylene, wherein the oligomer has: at least 93% allyl chain ends, an Mn of about 500 to about 20,000 g/mol (as measured by 1H NMR), an isobutyl chain end to allylic vinyl group ratio of 0.8:1 to 1.35:1.0, and less than 1400 ppm aluminum.
This invention further relates to a propylene oligomer, comprising at least 50 mol % propylene and from 10 to 50 mol % ethylene, wherein the oligomer has: at least 90% allyl chain ends, Mn of about 150 to about 10,000 g/mol (as measured by 1H NMR), and an isobutyl chain end to allylic vinyl group ratio of 0.8:1 to 1.3:1.0, wherein monomers having four or more carbon atoms are present at from 0 to 3 mol %.
This invention further relates to a propylene oligomer, comprising at least 50 mol % propylene, from 0.1 to 45 mol % ethylene, and from 0.1 to 5 mol % C4 to C12 olefin, wherein the oligomer has: at least 87% allyl chain ends (alternately at least 90%), an Mn of about 150 to about 10,000 g/mol, (as measured by 1H NMR), and an isobutyl chain end to allylic vinyl group ratio of 0.8:1 to 1.35:1.0.
This invention further relates to a propylene oligomer, comprising at least 50 mol % propylene, from 0.1 to 45 mol % ethylene, and from 0.1 to 5 mol % diene, wherein the oligomer has: at least 90% allyl chain ends, an Mn of about 150 to about 10,000 g/mol (as measured by 1H NMR), and an isobutyl chain end to allylic vinyl group ratio of 0.7:1 to 1.35:1.0.
This invention further relates to a homooligomer, comprising propylene, wherein the oligomer has: at least 93% allyl chain ends, an Mn of about 500 to about 20,000 g/mol (as measured by 1H NMR), an isobutyl chain end to allylic vinyl group ratio of 0.8:1 to 1.2:1.0, and less than 1400 ppm aluminum.
This invention further relates to a homogeneous process to make such oligomers.



BRIEF DESCRIPTION OF THE DRAWINGS
FIG. 1 is a plot of percent allylic chain ends versus mole % ethylene for Examples 35 and 52 to 61. (The triangles are data from Macromolecules 2008, 41, 559-567. The squares represent Examples 52 to 61 and the circle represents Example 35.)
FIG. 2 is a chart of the range of chemical shift assignments for the isobutyl chain ends for the E-P copolymers.



DETAILED DESCRIPTION
This invention relates to a propylene homo oligomer, comprising propylene and less than 0.5 wt % comonomer, preferably 0 wt % comonomer, wherein the oligomer has:

    
    
        i) at least 93% allyl chain ends (preferably at least 95%, preferably at least 97%, preferably at least 98%);
        ii) a number average molecular weight (Mn) of about 500 to about 20,000 g/mol, as measured by 1H NMR (preferably 500 to 15,000, preferably 700 to 10,000, preferably 800 to 8,000 g/mol, preferably 900 to 7,000, preferably 1000 to 6,000, preferably 1000 to 5,000);
        iii) an isobutyl chain end to allylic vinyl group ratio of 0.8:1 to 1.3:1.0;
        iv) less than 1400 ppm aluminum, (preferably less than 1200 ppm, preferably less than 1000 ppm, preferably less than 500 ppm, preferably less than 100 ppm).
    
    


This invention relates to a propylene co-oligomer having an Mn of 300 to 30,000 g/mol as measured by 1H NMR (preferably 400 to 20,000, preferably 500 to 15,000, preferably 600 to 12,000, preferably 800 to 10,000, preferably 900 to 8,000, preferably 900 to 7,000 g/mol), comprising 10 to 90 mol % propylene (preferably 15 to 85 mol %, preferably 20 to 80 mol %, preferably 30 to 75 mol %, preferably 50 to 90 mol %) and 10 to 90 mol % (preferably 85 to 15 mol %, preferably 20 to 80 mol %, preferably 25 to 70 mol %, preferably 10 to 50 mol %) of one or more alpha-olefin comonomers (preferably ethylene, butene, hexene, or octene, preferably ethylene), wherein the oligomer has at least X % allyl chain ends (relative to total unsaturations), where: 1) X=(−0.94(mole % ethylene incorporated)+100 {alternately 1.20 (−0.94(mole % ethylene incorporated)+100), alternately 1.50(−0.94(mole % ethylene incorporated)+100)}), when 10 to 60 mole % ethylene is present in the co-oligomer, and 2) X=45 (alternately 50, alternately 60), when greater than 60 and less than 70 mole % ethylene is present in the co-oligomer, and 3) X=(1.83*(mole % ethylene incorporated)−83, {alternately 1.20 [1.83*(mole % ethylene incorporated)−83], alternately 1.50 [1.83*(mole % ethylene incorporated)−83]}), when 70 to 90 mole % ethylene is present in the co-oligomer.
Alternately X is 80% or more, preferably 85% or more, preferably 90% or more, preferably 95% or more.
In an alternate embodiment the oligomer has at least 80% isobutyl chain ends (based upon the sum of isobutyl and n-propyl saturated chain ends), preferably at least 85% isobutyl chain ends, preferably at least 90% isobutyl chain ends. Alternately, the oligomer has an isobutyl chain end to allylic vinyl group ratio of 0.8:1 to 1.35:1.0, preferably 0.9:1 to 1.20:1.0, preferably 0.9:1.0 to 1.1:1.0.
This invention relates to a propylene oligomer, comprising more than 90 mol % propylene (preferably 95 to 99 mol %, preferably 98 to 9 mol %) and less than 10 mol % ethylene (preferably 1 to 4 mol %, preferably 1 to 2 mol %), wherein the oligomer has:
at least 93% allyl chain ends (preferably at least 95%, preferably at least 97%, preferably at least 98%);
a number average molecular weight (Mn) of about 400 to about 30,000 g/mol, as measured by 1H NMR (preferably 500 to 20,000, preferably 600 to 15,000, preferably 700 to 10,000 g/mol, preferably 800 to 9,000, preferably 900 to 8,000, preferably 1000 to 6,000);
an isobutyl chain end to allylic vinyl group ratio of 0.8:1 to 1.35:1.0, and
less than 1400 ppm aluminum, (preferably less than 1200 ppm, preferably less than 1000 ppm, preferably less than 500 ppm, preferably less than 100 ppm).
This invention also relates to a propylene oligomer, comprising:
at least 50 (preferably 60 to 90, preferably 70 to 90) mol % propylene and from 10 to 50 (preferably 10 to 40, preferably 10 to 30) mol % ethylene, wherein the oligomer has:
at least 90% allyl chain ends (preferably at least 91%, preferably at least 93%, preferably at least 95%, preferably at least 98%);
an Mn of about 150 to about 20,000 g/mol, as measured by 1H NMR (preferably 200 to 15,000, preferably 250 to 15,000, preferably 300 to 10,000, preferably 400 to 9,500, preferably 500 to 9,000, preferably 750 to 9,000); and
an isobutyl chain end to allylic vinyl group ratio of 0.8:1 to 1.3:1.0, wherein monomers having four or more carbon atoms are present at from 0 to 3 mol % (preferably at less than 1 mol %, preferably less than 0.5 mol %, preferably at 0 mol %).
This invention further relates to a propylene oligomer, comprising:
at least 50 (preferably at least 60, preferably 70 to 99.5, preferably 80 to 99, preferably 90 to 98.5) mol % propylene, from 0.1 to 45 (preferably at least 35, preferably 0.5 to 30, preferably 1 to 20, preferably 1.5 to 10) mol % ethylene, and from 0.1 to 5 (preferably 0.5 to 3, preferably 0.5 to 1) mol % C4 to C12 olefin (such as butene, hexene or octene, preferably butene), wherein the oligomer has:
at least 90% allyl chain ends (preferably at least 91%, preferably at least 93%, preferably at least 95%, preferably at least 98%);
a number average molecular weight (Mn) of about 150 to about 15,000 g/mol, as measured by 1H NMR (preferably 200 to 12,000, preferably 250 to 10,000, preferably 300 to 10,000, preferably 400 to 9500, preferably 500 to 9,000, preferably 750 to 9,000); and
an isobutyl chain end to allylic vinyl group ratio of 0.8:1 to 1.35:1.0.
This invention further relates to a propylene oligomer, comprising:
at least 50 (preferably at least 60, preferably 70 to 99.5, preferably 80 to 99, preferably 90 to 98.5) mol % propylene, from 0.1 to 45 (preferably at least 35, preferably 0.5 to 30, preferably 1 to 20, preferably 1.5 to 10) mol % ethylene, and from 0.1 to 5 (preferably 0.5 to 3, preferably 0.5 to 1) mol % diene (such as C4 to C12 alpha-omega dienes (such as butadiene, hexadiene, octadiene), norbornene, ethylidene norbornene, vinylnorbornene, norbornadiene, and dicyclopentadiene), wherein the oligomer has:
at least 90% allyl chain ends (preferably at least 91%, preferably at least 93%, preferably at least 95%, preferably at least 98%);
a number average molecular weight (Mn) of about 150 to about 20,000 g/mol, as measured by 1H NMR (preferably 200 to 15,000, preferably 250 to 12,000, preferably 300 to 10,000, preferably 400 to 9,500, preferably 500 to 9,000, preferably 750 to 9,000); and
an isobutyl chain end to allylic vinyl group ratio of 0.7:1 to 1.35:1.0.
Any of the oligomers prepared herein preferably have less than 1400 ppm aluminum, preferably less than 1000 ppm aluminum, preferably less than 500 ppm aluminum, preferably less than 100 ppm aluminum, preferably less than 50 ppm aluminum, preferably less than 20 ppm aluminum, preferably less than 5 ppm aluminum.
This invention also relates to a homogeneous process, preferably a bulk process, to make such oligomers.
As used herein, the term “oligomer” is defined to have an Mn of from 100 to 25,000 g/mol as measured by 1H NMR. When an oligomer is referred to as comprising an olefin, the olefin present in the oligomer is the oligomerized form of the olefin. A propylene oligomer is an oligomer having at least 50 mole % of propylene. A co-oligomer is an oligomer comprising at least two different monomer units (such as propylene and ethylene). A homo-oligomer is an oligomer comprising units of the same monomer (such as propylene). As used herein, Mn is number average molecular weight (measured by 1H NMR unless stated otherwise, as for example in Table 3A), Mw is weight average molecular weight (measured by Gel Permeation Chromatography), and Mz is z average molecular weight (measured by Gel Permeation Chromatography), wt % is weight percent, and mol % is mole percent. Molecular weight distribution (MWD) is defined to be Mw (measured by Gel Permeation Chromatography) divided by Mn (measured by 1H NMR). Unless otherwise noted, all molecular weight units (e.g., Mw, Mn, Mz) are g/mol.
“Allyl chain ends” is defined to be an oligomer having at least one terminus represented by (CH2CH—CH2-oligomer), formula I:




where the “••••” represents the oligomer chain. In a preferred embodiment the allyl chain ends is represented by the formula II:





The amount of allyl chain ends is determined using 1H NMR at 120° C. using deuterated tetrachloroethane as the solvent on a 500 MHz machine. and in selected cases confirmed by 13C NMR. Resconi has reported proton and carbon assignments (neat perdeuterated tetrachloroethane used for proton spectra while a 50:50 mixture of normal and perdeuterated tetrachloroethane was used for carbon spectra; all spectra were recorded at 100° C. on a Bruker AM 300 spectrometer operating at 300 MHz for proton and 75.43 MHz for carbon) for vinyl terminated propylene oligomers in J American Chemical Soc 114 1992, 1025-1032 that are useful herein.

“Isobutyl chain end” is defined to be an oligomer having at least one terminus represented by the formula:




where M represents the oligomer chain. In a preferred embodiment, the isobutyl chain end is represented by one of the following formulae:





where M represents the oligomer chain.

The percentage of isobutyl end groups is determined using 13C NMR (as described in the example section) and the chemical shift assignments in Resconi et al, J. Am. Chem. Soc. 1992, 114, 1025-1032 for 100% propylene oligomers and set forth in FIG. 2 for E-P oligomers.
The “isobutyl chain end to allylic vinyl group ratio” is defined to be the ratio of the percentage of isobutyl chain ends to the percentage of allylic vinyl groups.
In a preferred embodiment, the propylene oligomer comprises less than 3 wt % of functional groups selected from hydroxide, aryls and substituted aryls, halogens, alkoxys, carboxylates, esters, acrylates, oxygen, nitrogen, and carboxyl, preferably less than 2 wt %, more preferably less than 1 wt %, more preferably less than 0.5 wt %, more preferably less than 0.1 wt %, more preferably 0 wt %, based upon the weight of the oligomer.
The oligomer preferably has an M. as determined by 1H NMR of 150 to 25,000 g/mole, 200 to 20,000 g/mol, preferably 250 to 15,000 g/mol, preferably 300 to 15,000 g/mol, preferably 400 to 12,000 g/mol, preferably 750 to 10,000 g/mol. Further a desirable molecular weight range can be any combination of any upper molecular weight limit with any lower molecular weight limit described above. Mn is determined according to the methods described below in the examples section.
The oligomer preferably has a glass transition temperature (Tg) of 0° C. or less (as determined by differential scanning calorimetry as described below), preferably −10° C. or less, more preferably −20° C. or less, more preferably −30° C. or less, more preferably −50° C. or less.
The oligomer preferably contains less than 80 weight % of C4 olefin(s), (such as isobutylene n-butene, 2-butene, isobutylene, and butadiene), based upon the weight of the oligomer, preferably less than 10 wt %, preferably 5 wt %, preferably less than 4 wt %, preferably less than 3 wt %, preferably less than 2 wt %, preferably less than 1 wt %, preferably less than 0.5 wt %, preferably less than 0.25 wt % of C4 olefin(s) based upon the weight of the oligomer.
Alternately, the oligomer preferably contains less than 20 weight % of C4 or more olefin(s), (such as C4 to C30 olefins, typically such as C4 to C12 olefins, typically such as C4, C6, C8, C12, olefins, etc.), based upon the weight of the oligomer, preferably less than 10 wt %, preferably 5 wt %, preferably less than 4 wt %, preferably less than 3 wt %, preferably less than 2 wt %, preferably less than 1 wt %, preferably less than 0.5 wt %, preferably less than 0.25 wt % of C4 olefin(s) based upon the weight of the oligomer, as determined by 13C NMR.
In another embodiment, the oligomer composition produced comprises at least 50 wt % (preferably at least 75 wt %, preferably at least 90 wt %, based upon the weight of the oligomer composition) olefins having at least 36 carbon atoms (preferably at least 51 carbon atoms, preferably at least 102 carbon atoms) as measured by 1H NMR assuming one unsaturation per chain.
In another embodiment, the oligomer composition produced comprises less than 20 wt % dimer and trimer (preferably less than 10 wt %, preferably less than 5 wt %, more preferably less than 2 wt %, based upon the weight of the oligomer composition), as measured by GC.
In another embodiment, the oligomer produced here contains less than 25 ppm hafnium, preferably less than 10 ppm hafnium, preferably less than 5 ppm hafnium based on the yield of polymer produced and the mass of catalyst employed.
In another embodiment, the oligomers described herein may have a melting point (DSC first melt) of from 60 to 130° C., alternately 50 to 100° C. In another embodiment, the oligomers described herein have no detectable melting point by DSC following storage at ambient temperature (23° C.) for at least 48 hours.
Melting temperature (Tm) and glass transition temperature (Tg) are measured using Differential Scanning calorimetry (DSC) using commercially available equipment such as a TA Instruments 2920 DSC. Typically, 6 to 10 mg of the sample, that has been stored at room temperature for at least 48 hours, is sealed in an aluminum pan and loaded into the instrument at room temperature. The sample is equilibrated at 25° C., then it is cooled at a cooling rate of 10° C./min to −80° C. The sample is held at −80° C. for 5 min and then heated at a heating rate of 10° C./min to 25° C. The glass transition temperature is measured from the heating cycle. Alternatively, the sample is equilibrated at 25° C., then heated at a heating rate of 10° C./min to 150° C. The endothermic melting transition, if present, is analyzed for onset of transition and peak temperature. The melting temperatures reported are the peak melting temperatures from the first heat unless otherwise specified. For samples displaying multiple peaks, the melting point (or melting temperature) is defined to be the peak melting temperature (i.e., associated with the largest endothermic calorimetric response in that range of temperatures) from the DSC melting trace.
In another embodiment, the oligomers described herein are a liquid at 25° C.
In another embodiment, the oligomers described herein have an Mw (measured as described below) of 1,000 to about 30,000 g/mol, alternately 2000 to 25,000 g/mol, alternately 3,000 to 20,000 g/mol and/or an Mz of about 1700 to about 150,000 g/mol, alternately 800 to 100,000 g/mol.
Mw and Mz are measured by using a High Temperature Size Exclusion Chromatograph (either from Waters Corporation or Polymer Laboratories), equipped with a differential refractive index detector (DRI), Experimental details, are described in: T. Sun, P. Brant, R. R. Chance, and W. W. Graessley, Macromolecules, Volume 34, Number 19, 6812-6820, (2001) and references therein. Three Polymer Laboratories PLgel 10 mm Mixed-B columns are used. The nominal flow rate is 0.5 cm3/min, and the nominal injection volume is 300 μl. The various transfer lines, columns and differential refractometer (the DRI detector) are contained in an oven maintained at 135° C. Solvent for the SEC experiment is prepared by dissolving 6 grams of butylated hydroxy toluene as an antioxidant in 4 liters of Aldrich reagent grade 1, 2, 4 trichlorobenzene (TCB). The TCB mixture is then filtered through a 0.7 μm glass pre-filter and subsequently through a 0.1 μm Teflon filter. The TCB is then degassed with an online degasser before entering the SEC. Polymer solutions are prepared by placing dry polymer in a glass container, adding the desired amount of TCB, then heating the mixture at 160° C. with continuous agitation for about 2 hours. All quantities are measured gravimetrically. The TCB densities used to express the polymer concentration in mass/volume units are 1.463 g/ml at room temperature and 1.324 g/ml at 135° C. The injection concentration is from 1.0 to 2.0 mg/ml, with lower concentrations being used for higher molecular weight samples. Prior to running each sample the DRI detector and the injector are purged. Flow rate in the apparatus is then increased to 0.5 ml/minute, and the DRI is allowed to stabilize for 8 to 9 hours before injecting the first sample. The concentration, c, at each point in the chromatogram is calculated from the baseline-subtracted DRI signal, IDRI, using the following equation:

c=KDRIIDRI/(dn/dc)

where KDRI is a constant determined by calibrating the DRI, and (dn/dc) is the refractive index increment for the system. The refractive index, n=1.500 for TCB at 135° C. and λ=690 nm. For purposes of this invention and the claims thereto (dn/dc)=0.104 for propylene polymers and 0.1 otherwise. Units on parameters throughout this description of the SEC method are such that concentration is expressed in g/cm3, molecular weight is expressed in g/mole, and intrinsic viscosity is expressed in dL/g.

Molecular weight distribution (Mw/Mn—by GPC-DRI) is determined by the method above. In some embodiments, the oligomers of this invention have an Mw/Mn (by GPC-DRI) of 1.5 to 20, alternately 1.7 to 10.
Oligomerization Process
This invention also relates to a homogeneous process, preferably a bulk process, to make the oligomers described herein. In a preferred embodiment, propylene and optional comonomers (such as ethylene) can be oligomerized by reacting a catalyst system (comprising metallocene compound(s), and one or more activators) with the olefins. Other additives may also be used, as desired, such as scavengers and/or hydrogen. Any conventional suspension, homogeneous bulk, solution, slurry, or high-pressure oligomerization process can be used. Such processes can be run in a batch, semi-batch, or continuous mode. Such processes and modes are well known in the art. Homogeneous polymerization processes are preferred. (A homogeneous polymerization process is defined to be a process where at least 90 wt % of the product is soluble in the reaction media.) A bulk homogeneous process is particularly preferred. (A bulk process is defined to be a process where monomer concentration in all feeds to the reactor is 70 volume % or more.) Alternately no solvent or diluent is present or added in the reaction medium, (except for the small amounts used as the carrier for the catalyst system or other additives, or amounts typically found with the monomer; e.g. propane in propylene).
Suitable diluents/solvents for oligomerization include non-coordinating, inert liquids. Examples include straight and branched-chain hydrocarbons such as isobutane, butane, pentane, isopentane, hexanes, isohexane, heptane, octane, dodecane, and mixtures thereof; cyclic and alicyclic hydrocarbons such as cyclohexane, cycloheptane, methylcyclohexane, methylcycloheptane, and mixtures thereof such as can be found commercially (Isopars); perhalogenated hydrocarbons such as perfluorinated C4-10 alkanes, chlorobenzene, and aromatic and alkylsubstituted aromatic compounds such as benzene, toluene, mesitylene, and xylene. Suitable solvents also include liquid olefins which may act as monomers or comonomers including ethylene, propylene, 1-butene, 1-hexene, 1-pentene, 3-methyl-1-pentene, 4-methyl-1-pentene, 1-octene, and 1-decene. Mixtures of the foregoing are also suitable.
In a preferred embodiment, the feed concentration for the oligomerization is 60 volume % solvent or less, preferably 40 volume % or less, preferably 20 volume % or less. Preferably the oligomerization is run in a bulk process.
Suitable additives to the oligomerization process can include one or more scavengers, promoters, modifiers, reducing agents, oxidizing agents, hydrogen, aluminum alkyls, or silanes.
In a preferred embodiment hydrogen is present in the oligomerization reactor at a partial pressure of 0.001 to 50 psig, preferably from 0.01 to 25 psig, more preferably 0.1 to 10 psig. It has been found that in the present systems, hydrogen can be used to provide increased activity without significantly impairing the catalyst's ability to produce allylic chain ends. Preferably the catalyst activity (calculated as g/mmolcatalyst/hr) is at least 20% higher than the same reaction without hydrogen present, preferably at least 50% higher, preferably at least 100% higher.
In an alternate embodiment, the productivity at least 4500 g/mmol/hour, preferably 5000 or more g/mmol/hour, preferably 10,000 or more g/mmol/hr, preferably 50,000 or more g/mmol/hr.
In an alternate embodiment, the productivity is at least 80,000 g/mmol/hr, preferably at least 150,000 g/mmol/hr, preferably at least 200,000 g/mmol/hr, preferably at least 250,000 g/mmol/hr, preferably at least 300,000 g/mmol/hr.
Preferred oligomerizations can be run at typical temperatures and/or pressures, such as from 25 to 150° C., preferably 40 to 120° C., preferably 45 to 80° C., and preferably from 0.35 to 10 MPa, preferably from 0.45 to 6 MPa, preferably from 0.5 to 4 MPa.
In a typical oligomerization, the residence time of the reaction is up to 60 minutes, preferably between 5 to 50 minutes, preferably 10 to 40 minutes.
Catalyst Compound
Catalyst compounds useful herein include one or more metallocene compound(s) represented by the formulae:




where

    Hf is hafnium;
    each X is, independently, selected from the group consisting of hydrocarbyl radicals having from 1 to 20 carbon atoms, hydrides, amides, alkoxides, sulfides, phosphides, halogens, dienes, amines, phosphines, ethers, or a combination thereof, preferably methyl, ethyl, propyl, butyl, phenyl, benzyl, chloride, bromide, iodide, (alternately two X's may form a part of a fused ring or a ring system);
    each Q is, independently carbon or a heteroatom, preferably C, N, P, S (preferably at least one Q is a heteroatom, alternately at least two Q's are the same or different heteroatoms, alternately at least three Q's are the same or different heteroatoms, alternately at least four Q's are the same or different heteroatoms);
    each R1 is, independently, hydrogen or a C1 to C8 alkyl group, preferably a C1 to C8 linear alkyl group, preferably methyl ethyl, propyl, butyl, pentyl, hexyl, heptyl or octyl, R1 may the same or different as R2;
    each R2 is, independently, hydrogen or a C1 to C8 alkyl group, preferably a C1 to C8 linear alkyl group, preferably methyl ethyl, propyl, butyl, pentyl, hexyl, heptyl or octyl, provided that at least one of R1 or R2 is not hydrogen, preferably both of R1 and R2 are not hydrogen, preferably R1 and/or R2 are not branched;
    each R3 is, independently, hydrogen, or a substituted or unsubstituted hydrocarbyl group having from 1 to 8 carbon atoms, preferably 1 to 6 carbon atoms, preferably a substituted or unsubstituted C1 to C8 linear alkyl group, preferably methyl ethyl, propyl, butyl, pentyl, hexyl, heptyl, octyl, provided however that at least three R3 groups are not hydrogen (alternately four R3 groups are not hydrogen, alternately five R3 groups are not hydrogen); {Alternately, when the catalyst compound is to used to make the homo-oligomer then each R3 is, independently, hydrogen, or a substituted or unsubstituted hydrocarbyl group having from 1 to 8 carbon atoms, preferably 1 to 6 carbon atoms, preferably a substituted or unsubstituted C1 to C8 linear alkyl group, preferably methyl ethyl, propyl, butyl, pentyl, hexyl, heptyl, octyl, provided however that: 1) all five R3 groups are methyl, or 2) four R3 groups are not hydrogen and at least one R3 group is a C2 to C8 substituted or unsubstituted hydrocarbyl (preferably at least two, three, four or five R3 groups are a C2 to C8 substituted or unsubstituted hydrocarbyl)};
    each R4 is, independently, hydrogen or a substituted or unsubstituted hydrocarbyl group, a heteroatom or heteroatom containing group, preferably a substituted or unsubstituted hydrocarbyl group having from 1 to 20 carbon atoms, preferably 1 to 8 carbon atoms, preferably a substituted or unsubstituted C1 to C8 linear alkyl group, preferably methyl ethyl, propyl, butyl, pentyl, hexyl, heptyl, octyl, substituted phenyl (such as propyl phenyl), phenyl, silyl, substituted silyl, (such as CH2SiR′, where R′ is a C1 to C12 hydrocarbyl, such as methyl, ethyl, propyl, butyl, phenyl);
    R5 is hydrogen or a C1 to C8 alkyl group, preferably a C1 to C8 linear alkyl group, preferably methyl, ethyl, propyl, butyl, pentyl, hexyl, heptyl or octyl;
    R6 is hydrogen or a C1 to C8 alkyl group, preferably a C1 to C8 linear alkyl group, preferably methyl, ethyl, propyl, butyl, pentyl, hexyl, heptyl or octyl;
    each R7 is, independently, hydrogen, or a C1 to C8 alkyl group, preferably a C1 to C8 linear alkyl group, preferably methyl ethyl, propyl, butyl, pentyl, hexyl, heptyl or octyl, provided however that at least seven R7 groups are not hydrogen, alternately at least eight R7 groups are not hydrogen, alternately all R7 groups are not hydrogen, (preferably the R7 groups at the 3 and 4 positions on each Cp ring of Formula IV are not hydrogen);
    N is nitrogen;
    T is a bridge, preferably, Si or Ge, preferably Si;
    each Ra, is independently, hydrogen, halogen or a C1 to C20 hydrocarbyl, such as methyl, ethyl, propyl, butyl, pentyl, hexyl, heptyl, octyl, phenyl, benzyl, substituted phenyl, and two Ra can form a cyclic structure including aromatic, partially saturated, or saturated cyclic or fused ring system;

and further provided that any two adjacent R groups may form a fused ring or multicenter fused ring system where the rings may be aromatic, partially saturated or saturated.



The term “substituted” means that a hydrogen group has been replaced with a hydrocarbyl group, a heteroatom or a heteroatom containing group. For example methyl cyclopentadiene (Cp) is a Cp group substituted with a methyl group and ethyl alcohol is an ethyl group substituted with an —OH group.
In an alternate embodiment, at least one R4 group is not hydrogen, alternately at least two R4 groups are not hydrogen, alternately at least three R4 groups are not hydrogen, alternately at least four R4 groups are not hydrogen, alternately all R4 groups are not hydrogen.
Catalyst compounds that are particularly useful in this invention include one or more of:

    (1,3-Dimethylindenyl)(pentamethylcyclopentadienyl)Hafniumdimethyl,
    (1,3,4,7-Tetramethylindenyl)(pentamethylcyclopentadienyl)Hafniumdimethyl,
    (1,3-Dimethylindenyl)(tetramethylcyclopentadienyl)Hafniumdimethyl,
    (1,3-Diethylindenyl)(pentamethylcyclopentadienyl)Hafniumdimethyl,
    (1,3-Dipropylindenyl)(pentamethylcyclopentadienyl)Hafniumdimethyl,
    (1-Methyl,3-propyllindenyl)(pentamethylcyclopentadienyl)Hafniumdimethyl,
    (1,3-Dimethylindenyl)(tetramethylpropylcyclopentadienyl)Hafniumdimethyl,
    (1,2,3-Trimethylindenyl)(pentamethylcyclopentadienyl)Hafniumdimethyl,
    (1,3-Dimethylbenzindenyl)(pentamethylcyclopentadienyl)Hafniumdimethyl,
    (2,7-Bis t-butylfluorenyl)(pentamethylcyclopentadienyl)Hafniumdimethyl,
    (9-Methylfluorenyl)(pentamethylcyclopentadienyl)Hafniumdimethyl,
    (2,7,9-Trimethylfluorenyl)(pentamethylcyclopentadienyl)Hafniumdimethyl,
    μ-Dihydrosilyl(bis tetramethylcyclopentadienyl)Hafniumdimethyl,
    μ-Dihydrosilyl(bis tetramethylcyclopentadienyl)Hafniumdimethyl,
    μ-Dimethylsilyl(tetramethylcyclopentadienyl)(3-propyltrimethylcyclopentadienyl)Hafniumdimethyl, and
    μ-Dicyclopropylsilyl(bis tetramethylcyclopentadienyl)Hafniumdimethyl.


In an alternate embodiment, the “dimethyl” after the transition metal in the list of catalyst compounds above is replaced with a dihalide (such as dichloride or difluoride) or a bisphenoxide, particularly for use with an alumoxane activator.
Activators and Activation Methods for Catalyst Compounds
The terms “cocatalyst” and “activator” are used herein interchangeably and are defined to be any compound which can activate any one of the catalyst compounds described above by converting the neutral catalyst compound to a catalytically active catalyst compound cation. Non-limiting activators, for example, include alumoxanes, aluminum alkyls, ionizing activators, which may be neutral or ionic, and conventional-type cocatalysts. Preferred activators typically include alumoxane compounds, modified alumoxane compounds, and ionizing anion precursor compounds that abstract one reactive, σ-bound, metal ligand making the metal complex cationic and providing a charge-balancing noncoordinating or weakly coordinating anion.
In one embodiment, alumoxane activators are utilized as an activator in the catalyst composition. Alumoxanes are generally oligomeric compounds containing —Al(R1)—O— sub-units, where R1 is an alkyl group. Examples of alumoxanes include methylalumoxane (MAO), modified methylalumoxane (MMAO), ethylalumoxane and isobutylalumoxane. Alkylalumoxanes and modified alkylalumoxanes are suitable as catalyst activators, particularly when the abstractable ligand is an alkyl, halide, alkoxide or amide. Mixtures of different alumoxanes and modified alumoxanes may also be used. It may be preferable to use a visually clear methylalumoxane. A cloudy or gelled alumoxane can be filtered to produce a clear solution or clear alumoxane can be decanted from the cloudy solution. Another alumoxane is a modified methyl alumoxane (MMAO) cocatalyst type 3A (commercially available from Akzo Chemicals, Inc. under the trade name Modified Methylalumoxane type 3A, covered under patent number U.S. Pat. No. 5,041,584).
When the activator is an alumoxane (modified or unmodified), some embodiments select the maximum amount of activator at a 5000-fold molar excess Al/M over the catalyst precursor (per metal catalytic site). The minimum activator-to-catalyst-precursor is a 1:1 molar ratio. Alternate preferred ranges include up to 500:1, alternately up to 200:1, alternately up to 100:1 alternately from 1:1 to 50:1.
Aluminum alkyl or organoaluminum compounds which may be utilized as co-activators (or scavengers) include trimethylaluminum, triethylaluminum, triisobutylaluminum, tri-n-hexylaluminum, tri-n-octylaluminum and the like.
Ionizing Activators
It is within the scope of this invention to use an ionizing or stoichiometric activator, neutral or ionic, such as tri (n-butyl) ammonium tetrakis(pentafluorophenyl) borate, a tris perfluorophenyl boron metalloid precursor or a tris perfluoronapthyl boron metalloid precursor, polyhalogenated heteroborane anions (WO 98/43983), boric acid (U.S. Pat. No. 5,942,459) or combination thereof. It is also within the scope of this invention to use neutral or ionic activators alone or in combination with alumoxane or modified alumoxane activators. Much preferred activators are the ionic ones, not the neutral boranes.
Examples of neutral stoichiometric activators include tri-substituted boron, tellurium, aluminum, gallium and indium or mixtures thereof. The three substituent groups are each independently selected from alkyls, alkenyls, halogens, substituted alkyls, aryls, arylhalides, alkoxy and halides. Preferably, the three groups are independently selected from halogen, mono or multicyclic (including halosubstituted) aryls, alkyls, and alkenyl compounds and mixtures thereof, preferred are alkenyl groups having 1 to 20 carbon atoms, alkyl groups having 1 to 20 carbon atoms, alkoxy groups having 1 to 20 carbon atoms and aryl groups having 3 to 20 carbon atoms (including substituted aryls). More preferably, the three groups are alkyls having 1 to 4 carbon groups, phenyl, napthyl or mixtures thereof. Even more preferably, the three groups are halogenated, preferably fluorinated, aryl groups. Most preferably, the neutral stoichiometric activator is tris perfluorophenyl boron or tris perfluoronapthyl boron.
Ionic stoichiometric activator compounds may contain an active proton, or some other cation associated with, but not coordinated to, or only loosely coordinated to, the remaining ion of the ionizing compound. Such compounds and the like are described in European publications EP-A-0 570 982, EP-A-0 520 732, EP-A-0 495 375, EP-B1-0 500 944, EP-A-0 277 003 and EP-A-0 277 004, and U.S. Pat. Nos. 5,153,157, 5,198,401, 5,066,741, 5,206,197, 5,241,025, 5,384,299 and 5,502,124 and U.S. patent application Ser. No. 08/285,380, filed Aug. 3, 1994, all of which are herein fully incorporated by reference.
Ionic catalysts can be preparedly reacting a transition metal compound with some neutral Lewis acids, such as B(C6F6)3, which upon reaction with the hydrolyzable ligand (X) of the transition metal compound forms an anion, such as ([B(C6F5)3(X)]−), which stabilizes the cationic transition metal species generated by the reaction. The catalysts can be, and preferably are, prepared with activator components which are ionic compounds or compositions.
Compounds useful as an activator component in the preparation of the ionic catalyst systems used in the process of this invention comprise a cation, which is preferably a Bronsted acid capable of donating a proton, and a compatible non-coordinating anion which anion is relatively large (bulky), capable of stabilizing the active catalyst species (the Group 4 cation) which is formed when the two compounds are combined and said anion will be sufficiently labile to be displaced by olefinic, diolefinic and acetylenically unsaturated substrates or other neutral Lewis bases such as ethers, amines and the like. Two classes of compatible non-coordinating anions have been disclosed in EP-A0 277,003 and EP-A0 277,004 published 1988: 1) anionic coordination complexes comprising a plurality of lipophilic radicals covalently coordinated to and shielding a central charge-bearing metal or metalloid core, and 2) anions comprising a plurality of boron atoms such as carboranes, metallacarboranes and boranes.
In a preferred embodiment, the stoichiometric activators include a cation and an anion component, and may be represented by the following formula:

(L-H)d+(Ad−)  (14)

wherein L is an neutral Lewis base; H is hydrogen; (L-H)+ is a Bronsted acid; Ad− is a non-coordinating anion having the charge d-; and d is an integer from 1 to 3.

The cation component, (L-H)d+ may include Bronsted acids such as protonated Lewis bases capable of protonating a moiety, such as an alkyl or aryl, from the bulky ligand metallocene containing transition metal catalyst precursor, resulting in a cationic transition metal species.
The activating cation (L-H)d+ may be a Bronsted acid, capable of donating a proton to the transition metal catalytic precursor resulting in a transition metal cation, including ammoniums, oxoniums, phosphoniums, silyliums, and mixtures thereof, preferably ammoniums of methylamine, aniline, dimethylamine, diethylamine, N-methylaniline, diphenylamine, trimethylamine, triethylamine, N,N-dimethylaniline, methyldiphenylamine, pyridine, p-bromo N,N-dimethylaniline, p-nitro-N,N-dimethylaniline, phosphoniums from triethylphosphine, triphenylphosphine, and diphenylphosphine, oxoniums from ethers such as dimethyl ether diethyl ether, tetrahydrofuran and dioxane, sulfoniums from thioethers, such as diethyl thioethers and tetrahydrothiophene, and mixtures thereof.
The anion component Ad− include those having the formula [Mk+Qn]d− wherein k is an integer from 1 to 3; n is an integer from 2 to 6; n−k=d; M is an element selected from Group 13 of the Periodic Table of the Elements, preferably boron or aluminum, and Q is independently a hydride, bridged or unbridged dialkylamido, halide, alkoxide, aryloxide, hydrocarbyl, substituted hydrocarbyl, halocarbyl, substituted halocarbyl, and halosubstituted-hydrocarbyl radicals, said Q having up to 20 carbon atoms with the proviso that in not more than 1 occurrence is Q a halide. Preferably, each Q is a fluorinated hydrocarbyl group having 1 to 20 carbon atoms, more preferably each Q is a fluorinated aryl group, and most preferably each Q is a pentafluoryl aryl group. Examples of suitable Ad− also include diboron compounds as disclosed in U.S. Pat. No. 5,447,895, which is fully incorporated herein by reference.
Illustrative, but not limiting examples of boron compounds which may be used as an activating cocatalyst in the preparation of the improved catalysts of this invention are tri-substituted ammonium salts such as:

    trimethylammonium tetraphenylborate, triethylammonium tetraphenylborate, tripropylammonium tetraphenylborate, tri(n-butyl)ammonium tetraphenylborate, tri(t-butyl)ammonium tetraphenylborate, N,N-dimethylanilinium tetraphenylborate, N,N-diethylanilinium tetraphenylborate, N,N-dimethyl-(2,4,6-trimethylanilinium) tetraphenylborate, tropillium tetraphenylborate, triphenylcarbenium tetraphenylborate, triphenylphosphonium tetraphenylborate triethylsilylium tetraphenylborate, benzene(diazonium)tetraphenylborate, trimethylammonium tetrakis(pentafluorophenyl)borate, triethylammonium tetrakis(pentafluorophenyl)borate, tripropylammonium tetrakis(pentafluorophenyl)borate, tri(n-butyl)ammonium tetrakis(pentafluorophenyl)borate, tri(sec-butyl)ammonium tetrakis(pentafluorophenyl)borate, N,N-dimethylanilinium tetrakis(pentafluorophenyl)borate, N,N-diethylanilinium tetrakis(pentafluorophenyl)borate, N,N-dimethyl-(2,4,6-trimethylanilinium)tetrakis(pentafluorophenyl)borate, tropillium tetrakis(pentafluorophenyl)borate, triphenylcarbenium tetrakis(pentafluorophenyl)borate, triphenylphosphonium tetrakis(pentafluorophenyl)borate, triethylsilylium tetrakis(pentafluorophenyl)borate, benzene(diazonium)tetrakis(pentafluorophenyl)borate, trimethylammonium tetrakis-(2,3,4,6-tetrafluorophenyl) borate, triethylammonium tetrakis-(2,3,4,6-tetrafluorophenyl)borate, tripropylammonium tetrakis-(2,3,4,6-tetrafluorophenyl)borate, tri(n-butyl)ammonium tetrakis-(2,3,4,6-tetrafluoro-phenyl)borate, dimethyl(t-butyl)ammonium tetrakis-(2,3,4,6-tetrafluorophenyl)borate, N,N-dimethylanilinium tetrakis-(2,3,4,6-tetrafluorophenyl)borate, N,N-diethylanilinium tetrakis-(2,3,4,6-tetrafluorophenyl)borate, N,N-dimethyl-(2,4,6-trimethylanilinium)tetrakis-(2,3,4,6-tetrafluorophenyl)borate, tropillium tetrakis-(2,3,4,6-tetrafluorophenyl)borate, triphenylcarbenium tetrakis-(2,3,4,6-tetrafluorophenyl)borate, triphenylphosphonium tetrakis-(2,3,4,6-tetrafluorophenyl)borate, triethylsilylium tetrakis-(2,3,4,6-tetrafluorophenyl)borate, benzene(diazonium)tetrakis-(2,3,4,6-tetrafluorophenyl)borate, trimethylammonium tetrakis(perfluoronapthyl)borate, triethylamonium tetrakis(perfluoronapthyl)borate, tripropylammonium tetrakis(perfluoronapthyl)borate, tri(n-butyl)ammonium tetrakis(perfluoronapthyl)borate, tri(t-butyl)ammonium tetrakis(perfluoronapthyl)borate, N,N-dimethylanilinium tetrakis(perfluoronapthyl)borate, N,N-diethylanilinium tetrakis(perfluoronapthyl)borate, N,N-dimethyl-(2,4,6-trimethylanilinium)tetrakis(perfluoronapthyl)borate, tropillium tetrakis(perfluoronapthyl)borate, triphenylcarbenium tetrakis(perfluoronapthyl)borate, triphenylphosphonium tetrakis(perfluoronapthyl)borate, triethylsilylium tetrakis(perfluoronapthyl)borate, benzene(diazonium)tetrakis(perfluoronapthyl)borate, trimethylammonium tetrakis(perfluorobiphenyl)borate, triethylammonium tetrakis(perfluorobiphenyl)borate, tripropylammonium tetrakis(perfluorobiphenyl)borate, tri(n-butyl)ammonium tetrakis(perfluorobiphenyl)borate, tri(t-butyl)ammonium tetrakis(perfluorobiphenyl)borate, N,N-dimethylanilinium tetrakis(perfluorobiphenyl)borate, N,N-diethylanilinium tetrakis(perfluorobiphenyl)borate, N,N-dimethyl-(2,4,6-trimethylanilinium)tetrakis(perfluorobiphenyl)borate, tropillium tetrakis(perfluorobiphenyl)borate, triphenylcarbenium tetrakis(perfluorobiphenyl)borate, triphenylphosphonium tetrakis(perfluorobiphenyl)borate, triethylsilylium tetrakis(perfluorobiphenyl)borate, benzene(diazonium)tetrakis(perfluorobiphenyl)borate, trimethylammonium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, triethylammonium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, tripropylammonium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, tri(n-butyl)ammonium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, tri(t-butyl)ammonium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, N,N-dimethylanilinium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, N,N-diethylanilinium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, N,N-dimethyl-(2,4,6-trimethylanilinium)tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, tropillium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, triphenylcarbenium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, triphenylphosphonium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, triethylsilylium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, benzene(diazonium)tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, and dialkyl ammonium salts such as: di-(i-propyl)ammonium tetrakis(pentafluorophenyl)borate, and dicyclohexylammonium tetrakis(pentafluorophenyl)borate; and additional tri-substituted phosphonium salts such as tri(o-tolyl)phosphonium tetrakis(pentafluorophenyl)borate, and tri(2,6-dimethylphenyl)phosphonium tetrakis(pentafluorophenyl)borate.


Most preferably, the ionic stoichiometric activator (L-H)d+(Ad−) is, N,N-dimethylanilinium tetrakis(perfluoronapthyl)borate, N,N-dimethylanilinium tetrakis(perfluorobiphenyl)borate, N,N-dimethylanilinium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, triphenylcarbenium tetrakis(perfluoronapthyl)borate, triphenylcarbenium tetrakis(perfluorobiphenyl)borate, triphenylcarbenium tetrakis(3,5-bis(trifluoromethyl)phenyl)borate, or triphenylcarbenium tetrakis(perfluorophenyl)borate.
In one embodiment, an activation method using ionizing ionic compounds not containing an active proton but capable of producing a bulky ligand metallocene catalyst cation and their non-coordinating anion are also contemplated, and are described in EP-A 0 426 637, EP-A 0 573 403 and U.S. Pat. No. 5,387,568, which are all herein incorporated by reference.
The term “non-coordinating anion” (NCA) means an anion which either does not coordinate to said cation or which is only weakly coordinated to said cation thereby remaining sufficiently labile to be displaced by a neutral Lewis base. “Compatible” non-coordinating anions are those which are not degraded to neutrality when the initially formed complex decomposes. Further, the anion will not transfer an anionic substituent or fragment to the cation so as to cause it to form a neutral four coordinate metallocene compound and a neutral by-product from the anion. Non-coordinating anions useful in accordance with this invention are those that are compatible, stabilize the metallocene cation in the sense of balancing its ionic charge at +1, yet retain sufficient lability to permit displacement by an ethylenically or acetylenically unsaturated monomer during polymerization. In addition to these activator compounds or co-catalysts, scavengers are used such as tri-isobutyl aluminum or tri-octyl aluminum.
Invention process also can employ cocatalyst compounds or activator compounds that are initially neutral Lewis acids but form a cationic metal complex and a noncoordinating anion, or a zwitterionic complex upon reaction with the invention compounds. For example, tris(pentafluorophenyl) boron or aluminum act to abstract a hydrocarbyl or hydride ligand to yield an invention cationic metal complex and stabilizing noncoordinating anion, see EP-A 0 427 697 and EP-A 0 520 732 for illustrations of analogous Group-4 metallocene compounds. Also, see the methods and compounds of EP-A 0 495 375. For formation of zwitterionic complexes using analogous Group 4 compounds, see U.S. Pat. Nos. 5,624,878; 5,486,632; and 5,527,929.
Another suitable ion forming, activating cocatalyst comprises a salt of a cationic oxidizing agent and a noncoordinating, compatible anion represented by the formula:

(OXe+)d(Ad−)e  (16)

wherein OXe+ is a cationic oxidizing agent having a charge of e+; e is an integer from 1 to 3; and A−, and d are as previously defined. Examples of cationic oxidizing agents include: ferrocenium, hydrocarbyl-substituted ferrocenium, Ag+, or Pb+2. Preferred embodiments of Ad− are those anions previously defined with respect to the Bronsted acid containing activators, especially tetrakis(pentafluorophenyl)borate.

The typical NCA activator-to-catalyst-precursor ratio is a 1:1 molar ratio. Alternate preferred ranges include from 0.1:1 to 100:1, alternately from 0.5:1 to 200:1, alternately from 1:1 to 500:1 alternately from 1:1 to 1000:1. A particularly useful range is from 0.5:1 to 10:1, preferably 1:1 to 5:1.
Activator Combinations
It is within the scope of this invention that catalyst compounds can be combined with one or more activators or activation methods described above. For example, a combination of activators have been described in U.S. Pat. Nos. 5,153,157 and 5,453,410, European publication EP-B1 0 573 120, and PCT publications WO 94/07928 and WO 95/14044. These documents all discuss the use of an alumoxane in combination with an ionizing activator.
Oligomer Uses
The oligomers prepared herein may be functionalized by reacting a hereroatom containing group with the oligomer with or without a catalyst. Examples include catalytic hydrosilylation, hydroformylation, or hydroamination, or maleation with activators such as free radical generators (e.g. peroxides). The functionalized oligomers can be used in oil additivation and many other applications. Preferred uses include additives for lubricants and or fuels. Preferred heteroatom containing groups include, amines, aldehydes, alcohols, acids, succinic acid, maleic acid and maleic anhydride.
In some embodiments the oligomers produced herein are functionalized as described in U.S. Pat. No. 6,022,929; A. Toyota, T. Tsutsui, and N. Kashiwa, Polymer Bulletin 48, 213-219, 2002; and J. Am. Chem. Soc., 1990, 112, 7433-7434.
In another embodiment this invention relates to:

    1. A co-oligomer having an Mn of 300 to 30,000 g/mol comprising 10 to 90 mol % propylene and 10 to 90 mol % of ethylene, wherein the oligomer has at least X % allyl chain ends (relative to total unsaturations as measured by 1H NMR), where: 1) X=(−0.94(mole % ethylene incorporated)+100), when 10 to 60 mole % ethylene is present in the co-oligomer, and 2) X=45, when greater than 60 and less than 70 mole % ethylene is present in the co-oligomer, and 3) X=(1.83*(mole % ethylene incorporated)−83), when 70 to 90 mole % ethylene is present in the co-oligomer.
    2. The oligomer of paragraph 1 wherein the oligomer has more than 90% allyl chain ends (relative to total unsaturations).
    3. The oligomer of paragraph 1 wherein the oligomer comprises at 15 to 95 wt % ethylene and has more than 80% allyl chain ends (relative to total unsaturations).
    4. The oligomer of paragraph 1 wherein the oligomer comprises at 30 to 95 wt % ethylene and has more than 70% allyl chain ends (relative to total unsaturations).
    5. The oligomer of paragraph 1 wherein the oligomer comprises at 30 to 95 wt % ethylene and has more than 90% allyl chain ends (relative to total unsaturations).
    6. A propylene oligomer, comprising more than 90 mol % propylene and less than 10 mol % ethylene wherein the oligomer has: at least 93% allyl chain ends, a number average molecular weight (Mn) of about 500 to about 20,000 g/mol, an isobutyl chain end to allylic vinyl group ratio of 0.8:1 to 1.35:1.0, and less than 1400 ppm aluminum.
    7. A propylene oligomer, comprising: at least 50 mol % propylene and from 10 to 50 mol % ethylene, wherein the oligomer has: at least 90% allyl chain ends, an Mn of about 150 to about 10,000 g/mol, and an isobutyl chain end to allylic vinyl group ratio of 0.8:1 to 1.2:1.0, wherein monomers having four or more carbon atoms are present at from 0 to 3 mol %.
    8. A propylene oligomer, comprising at least 50 mol % propylene, from 0.1 to 45 mol % ethylene, and from 0.1 to 5 mol % C4 to C12 olefin, wherein the oligomer has: at least 90% allyl chain ends, an Mn of about 150 to about 10,000 g/mol, and an isobutyl chain end to allylic vinyl group ratio of 0.8:1 to 1.35:1.0.
    9. A propylene oligomer, comprising at least 50 mol % propylene, from 0.1 to 45 mol % ethylene, and from 0.1 to 5 mol % diene, wherein the oligomer has: at least 90% allyl chain ends, an Mn of about 150 to about 10,000 g/mol, and an isobutyl chain end to allylic vinyl group ratio of 0.7:1 to 1.35:1.0.
    10. A homo-oligomer, comprising propylene, wherein the oligomer has: at least 93% allyl chain ends, an Mn of about 500 to about 20,000 g/mol, an isobutyl chain end to allylic vinyl group ratio of 0.8:1 to 1.2:1.0, and less than 1400 ppm aluminum.
    11. The oligomer of any of paragraphs 1 to 10, wherein the oligomer is a liquid at 25° C.
    12. The oligomer of any of paragraphs 1-11, wherein the Mn is about 500 to about 7,500 g/mol, the Mw is 1,000 to about 20,000 g/mol, and the Mz is about 1400 (alternately 1700) to about 150,000 g/mol.
    13. The oligomer of any of paragraphs 1-12, wherein the oligomer has no detectable melting point by DSC following storage at ambient temperature for at least 48 hours.
    14. The oligomer of any of paragraphs 1-12, wherein the oligomer has a melting peak of from about 60° C. to about 130° C.
    15. A homogenous process for making the propylene co-oligomer of any of the above paragraphs 1 to 14, said process having productivity of at least 4.5×103 g/mmol/hr, wherein the process comprises:


contacting, at a temperature of from 35° C. to 150° C., propylene, 0.1 to 70 mol % ethylene and from 0 to about 5 wt % hydrogen in the presence of a catalyst system comprising an activator and at least one metallocene compound represented by the formulae:




where

    Hf is hafnium;
    each X is, independently, selected from the group consisting of hydrocarbyl radicals having from 1 to 20 carbon atoms, hydrides, amides, alkoxides, sulfides, phosphides, halogens, dienes, amines, phosphines, ethers, or a combination thereof, preferably methyl, ethyl, propyl, butyl, phenyl, benzyl, chloride, bromide, iodide, (alternately two X's may form a part of a fused ring or a ring system);
    each Q is, independently carbon or a heteroatom, preferably C, N, P, S (preferably at least one Q is a heteroatom, alternately at least two Q's are the same or different heteroatoms, alternately at least three Q's are the same or different heteroatoms, alternately at least four Q's are the same or different heteroatoms);
    each R1 is, independently, a C1 to C8 alkyl group, preferably a C1 to C8 linear alkyl group, preferably methyl ethyl, propyl, butyl, pentyl, hexyl, heptyl or octyl, R1 may the same or different as R2;
    each R2 is, independently, a C1 to C8 alkyl group, preferably a C1 to C8 linear alkyl group, preferably methyl ethyl, propyl, butyl, pentyl, hexyl, heptyl or octyl, preferably R1 and/or R2 are not branched;
    each R3 is, independently, hydrogen, or a substituted or unsubstituted hydrocarbyl group having from 1 to 8 carbon atoms, preferably 1 to 6 carbon atoms, preferably a substituted or unsubstituted C1 to C8 linear alkyl group, preferably methyl ethyl, propyl, butyl, pentyl, hexyl, heptyl, octyl, provided however that at least three R3 groups are not hydrogen (alternately four R3 groups are not hydrogen, alternately five R3 groups are not hydrogen);
    each R4 is, independently, hydrogen or a substituted or unsubstituted hydrocarbyl group, a heteroatom or heteroatom containing group, preferably a substituted or unsubstituted hydrocarbyl group having from 1 to 20 carbon atoms, preferably 1 to 8 carbon atoms, preferably a substituted or unsubstituted C1 to C8 linear alkyl group, preferably methyl ethyl, propyl, butyl, pentyl, hexyl, heptyl, octyl, substituted phenyl (such as propyl phenyl), phenyl, silyl, substituted silyl, (such as CH2SiR′, where R′ is a C1 to C12 hydrocarbyl, such as methyl, ethyl, propyl, butyl, phenyl);
    R5 is hydrogen or a C1 to C8 alkyl group, preferably a C1 to C8 linear alkyl group, preferably methyl, ethyl, propyl, butyl, pentyl, hexyl, heptyl or octyl;
    R6 is hydrogen or a C1 to C8 alkyl group, preferably a C1 to C8 linear alkyl group, preferably methyl, ethyl, propyl, butyl, pentyl, hexyl, heptyl or octyl;
    each R7 is, independently, hydrogen, or a C1 to C8 alkyl group, preferably a C1 to C8 linear alkyl group, preferably methyl ethyl, propyl, butyl, pentyl, hexyl, heptyl or octyl, provided however that at least seven R7 groups are not hydrogen, alternately at least eight R7 groups are not hydrogen, alternately all R7 groups are not hydrogen, (preferably the R7 groups at the 3 and 4 positions on each Cp ring of Formula IV are not hydrogen);
    N is nitrogen;
    T is a bridge, preferably, Si or Ge, preferably Si;
    each Ra, is independently, hydrogen, halogen or a C1 to C20 hydrocarbyl, such as methyl, ethyl, propyl, butyl, pentyl, hexyl, heptyl, octyl, phenyl, benzyl, substituted phenyl, and two Ra can form a cyclic structure including aromatic, partially saturated, or saturated cyclic or fused ring system;
    and further provided that any two adjacent R groups may form a fused ring or multicenter fused ring system where the rings may be aromatic, partially saturated or saturated.
    16. A homogenous process for making the propylene homo-oligomer of any of paragraphs 1 to 14, said process having a productivity of at least 4.5×106 g/mol/min, wherein the process comprises:


contacting, at a temperature of from 30° C. to 120° C., propylene, 0 mol % comonomer and from 0 to about 5 wt % hydrogen in the presence of a catalyst system comprising an activator and at least one metallocene compound represented by the formulae:




where

    Hf is hafnium;
    each X is, independently, selected from the group consisting of hydrocarbyl radicals having from 1 to 20 carbon atoms, hydrides, amides, alkoxides, sulfides, phosphides, halogens, dienes, amines, phosphines, ethers, or a combination thereof, preferably methyl, ethyl, propyl, butyl, phenyl, benzyl, chloride, bromide, iodide, (alternately two X's may form a part of a fused ring or a ring system);
    each Q is, independently carbon or a heteroatom, preferably C, N, P, S (preferably at least one Q is a heteroatom, alternately at least two Q's are the same or different heteroatoms, alternately at least three Q's are the same or different heteroatoms, alternately at least four Q's are the same or different heteroatoms);
    each R1 is, independently, a C1 to C8 alkyl group, preferably a C1 to C8 linear alkyl group, preferably methyl ethyl, propyl, butyl, pentyl, hexyl, heptyl or octyl, R1 may the same or different as R2;
    each R2 is, independently, a C1 to C8 alkyl group, preferably a C1 to C8 linear alkyl group, preferably methyl ethyl, propyl, butyl, pentyl, hexyl, heptyl or octyl, preferably R1 and/or R2 are not branched;
    each R3 is, independently, hydrogen, or a substituted or unsubstituted hydrocarbyl group having from 1 to 8 carbon atoms, preferably 1 to 6 carbon atoms, preferably a substituted or unsubstituted C1 to C8 linear alkyl group, preferably methyl ethyl, propyl, butyl, pentyl, hexyl, heptyl, octyl, provided however that: 1) all five R3 groups are methyl, or 2) four R3 groups are not hydrogen and at least one R3 group is a C2 to C8 substituted or unsubstituted hydrocarbyl (preferably at least two, three, four or five R3 groups are a C2 to C8 substituted or unsubstituted hydrocarbyl);
    each R4 is, independently, hydrogen or a substituted or unsubstituted hydrocarbyl group, a heteroatom or heteroatom containing group, preferably a substituted or unsubstituted hydrocarbyl group having from 1 to 20 carbon atoms, preferably 1 to 8 carbon atoms, preferably a substituted or unsubstituted C1 to C8 linear alkyl group, preferably methyl ethyl, propyl, butyl, pentyl, hexyl, heptyl, octyl, substituted phenyl (such as propyl phenyl), phenyl, silyl, substituted silyl, (such as CH2SiR′, where R′ is a C1 to C12 hydrocarbyl, such as methyl, ethyl, propyl, butyl, phenyl);
    R5 is hydrogen or a C1 to C8 alkyl group, preferably a C1 to C8 linear alkyl group, preferably methyl, ethyl, propyl, butyl, pentyl, hexyl, heptyl or octyl;
    R6 is hydrogen or a C1 to C8 alkyl group, preferably a C1 to C8 linear alkyl group, preferably methyl, ethyl, propyl, butyl, pentyl, hexyl, heptyl or octyl;
    each R7 is, independently, hydrogen, or a C1 to C8 alkyl group, preferably a C1 to C8 linear alkyl group, preferably methyl ethyl, propyl, butyl, pentyl, hexyl, heptyl or octyl, provided however that at least seven R7 groups are not hydrogen, alternately at least eight R7 groups are not hydrogen, alternately all R7 groups are not hydrogen, (preferably the R7 groups at the 3 and 4 positions on each Cp ring of Formula IV are not hydrogen);
    N is nitrogen;
    T is a bridge, preferably, Si or Ge, preferably Si;
    each Ra, is independently, hydrogen, halogen or a C1 to C20 hydrocarbyl, such as methyl, ethyl, propyl, butyl, pentyl, hexyl, heptyl, octyl, phenyl, benzyl, substituted phenyl, and two Ra can form a cyclic structure including aromatic, partially saturated, or saturated cyclic or fused ring system;
    and further provided that any two adjacent R groups may form a fused ring or multicenter fused ring system where the rings may be aromatic, partially saturated or saturated.
    17. The process of paragraph 15 or 16, wherein the activator comprises one or more non-coordinating anions.
    18. The process of paragraph 15, 16, or 17 wherein the catalyst system comprises one or more of (pentamethylcyclopentadienyl)(1,3 dimethylindenyl)hafnium)dimethyl, and (pentamethylcyclopentadienyl)(1,3 dimethylindenyl)hafnium)dichloride.
    19. The process of paragraph 15 or 17, wherein the catalyst system comprises one or more of (1,3-Dimethylindenyl)(pentamethylcyclopentadienyl)Hafniumdimethyl, (1,3,4,7-Tetramethylindenyl)(pentamethylcyclopentadienyl)Hafniumdimethyl, (1,3-Dimethylindenyl)(tetramethylcyclopentadienyl)Hafniumdimethyl, (1,3-Diethylindenyl)(pentamethylcyclopentadienyl)Hafniumdimethyl, (1,3-Dipropylindenyl)(pentamethylcyclopentadienyl)Hafniumdimethyl, (1-Methyl,3-propyllindenyl)(pentamethylcyclopentadienyl)Hafniumdimethyl, (1,3-Dimethylindenyl)(tetramethylpropylcyclopentadienyl)Hafniumdimethyl, (1,2,3-Trimethylindenyl)(pentamethylcyclopentadienyl)Hafniumdimethyl, (1,3-Dimethylbenzindenyl)(pentamethylcyclopentadienyl)Hafniumdimethyl, (2,7-Bis t-butylfluorenyl)(pentamethylcyclopentadienyl)Hafniumdimethyl, (9-Methylfluorenyl)(pentamethylcyclopentadienyl)Hafniumdimethyl, (2,7,9-Trimethylfluorenyl)(pentamethylcyclopentadienyl)Hafniumdimethyl, μ-Dihydrosilyl(bis tetramethylcyclopentadienyl)Hafniumdimethyl, μ-Dihydrosilyl(bis tetramethylcyclopentadienyl)Hafniumdimethyl, μ-Dimethylsilyl(tetramethylcyclopentadienyl)(3-propyltrimethylcyclopentadienyl) Hafniumdimethyl, μ-Dicyclopropylsilyl(bis tetramethylcyclopentadienyl)Hafnium dimethyl. (1,3-Dimethylindenyl)(pentamethylcyclopentadienyl)Hafniumdihalide, (1,3,4,7-Tetramethylindenyl)(pentamethylcyclopentadienyl)Hafniumdihalide, (1,3-Dimethylindenyl)(tetramethylcyclopentadienyl)Hafniumdihalide, (1,3-Diethylindenyl)(pentamethylcyclopentadienyl)Hafniumdihalide, (1,3-Dipropylindenyl)(pentamethylcyclopentadienyl)Hafniumdihalide, (1-Methyl,3-propyllindenyl)(pentamethylcyclopentadienyl)Hafniumdihalide, (1,3-Dimethylindenyl)(tetramethylpropylcyclopentadienyl)Hafniumdihalide, (1,2,3-Trimethylindenyl)(pentamethylcyclopentadienyl)Hafniumdihalide, (1,3-Dimethylbenzindenyl)(pentamethylcyclopentadienyl)Hafniumdihalide, (2,7-Bis t-butylfluorenyl)(pentamethylcyclopentadienyl)Hafniumdihalide, (9-Methylfluorenyl)(pentamethylcyclopentadienyl)Hafniumdihalide, (2,7,9-Trimethylfluorenyl)(pentamethylcyclopentadienyl)Hafniumdihalide, μ-Dihydrosilyl(bis tetramethylcyclopentadienyl)Hafniumdihalide, μ-Dihydrosilyl(bis tetramethylcyclopentadienyl)Hafniumdihalide, μ-Dihalidesilyhtetramethylcyclopentadienyl)(3-propyltrimethylcyclopentadienyl) Hafniumdihalide, and μ-Dicyclopropylsilyl(bis tetramethylcyclopentadienyl)Hafnium dihalide.
    20. The process of paragraph 16 or 17, wherein the catalyst system comprises one or more of (1,3-Dimethylindenyl)(pentamethylcyclopentadienyl)Hafniumdimethyl, (1,3,4,7-Tetramethylindenyl)(pentamethylcyclopentadienyl)Hafniumdimethyl, (1,3-Diethylindenyl)(pentamethylcyclopentadienyl)Hafniumdimethyl, (1,3-Dipropylindenyl)(pentamethylcyclopentadienyl)Hafniumdimethyl, (1-Methyl,3-propyllindenyl)(pentamethylcyclopentadienyl)Hafniumdimethyl, (1,2,3-Trimethylindenyl)(pentamethylcyclopentadienyl)Hafniumdimethyl, (1,3-Dimethylbenzindenyl)(pentamethylcyclopentadienyl)Hafniumdimethyl, (2,7-Bis t-butylfluorenyl)(pentamethylcyclopentadienyl)Hafniumdimethyl, (9-Methylfluorenyl)(pentamethylcyclopentadienyl)Hafniumdimethyl, (2,7,9-Trimethylfluorenyl)(pentamethylcyclopentadienyl)Hafniumdimethyl, (1,3-Dimethylindenyl)(pentamethylcyclopentadienyl)Hafniumdihalide, (1,3,4,7-Tetramethylindenyl)(pentamethylcyclopentadienyl)Hafniumdihalide, (1,3-Diethylindenyl)(pentamethylcyclopentadienyl)Hafniumdihalide, (1,3-Dipropylindenyl)(pentamethylcyclopentadienyl)Hafniumdihalide, (1-Methyl,3-propyllindenyl)(pentamethylcyclopentadienyl)Hafniumdihalide, (1,2,3-Trimethylindenyl)(pentamethylcyclopentadienyl)Hafniumdihalide, (1,3-Dimethylbenzindenyl)(pentamethylcyclopentadienyl)Hafniumdihalide, (2,7-Bis t-butylfluorenyl)(pentamethylcyclopentadienyl)Hafniumdihalide, (9-Methylfluorenyl)(pentamethylcyclopentadienyl)Hafniumdihalide, and (2,7,9-Trimethylfluorenyl)(pentamethylcyclopentadienyl)Hafniumdihalide.
    21. The process of any of paragraphs 15 to 20, further comprising functionalizing the propylene oligomer.
    22. The process of any of paragraphs 15 to 20, further comprising functionalizing the propylene oligomer with succinic acid, maleic acid, maleic anhydride or combinations thereof.


EXAMPLES
The foregoing discussion can be further described with reference to the following non-limiting examples.
Product Characterization
Products were characterized by 1H NMR and 13C NMR as follows:
13C NMR
13C NMR data was collected at 120° C. in a 10 mm probe using a Varian spectrometer with a 1Hydrogen frequency of at least 400 MHz. A 90 degree pulse, an acquisition time adjusted to give a digital resolution between 0.1 and 0.12 Hz, at least a 10 second pulse acquisition delay time with continuous broadband proton decoupling using swept square wave modulation without gating was employed during the entire acquisition period. The spectra were acquired using time averaging to provide a signal to noise level adequate to measure the signals of interest. Samples were dissolved in tetrachloroethane-d2 at concentrations between 10 to 15 wt % prior to being inserted into the spectrometer magnet.
Prior to data analysis spectra were referenced by setting the chemical shift of the (—CH2—)n signal where n>6 to 29.9 ppm.
Chain ends for quantization were identified using the signals shown in the table below. N-butyl and n-propyl were not reported due to their low abundance (less than 5%) relative to the chain ends shown in the table below.














Chain End
13CNMR Chemical Shift









P~i-Bu
23-5 to 25.5 and 25.8 to 26.3 ppm



E~i-Bu
39.5 to 40.2 ppm



P~Vinyl
41.5 to 43 ppm



E~Vinyl
33.9 to 34.4 ppm










1H NMR

1H NMR data was collected at either room temperature or 120° C. (for purposes of the claims, 120° C. shall be used) in a 5 mm probe using a Varian spectrometer with a 1Hydrogen frequency of at least 400 MHz. Data was recorded using a maximum pulse width of 45° C., 8 seconds between pulses and signal averaging 120 transients. Spectral signals were integrated and the number of unsaturation types per 1000 carbons was calculated by multiplying the different groups by 1000 and dividing the result by the total number of carbons. Mn was calculated by dividing the total number of unsaturated species into 14,000.
The chemical shift regions for the olefin types are defined to be between the following spectral regions.












Unsaturation Type
Region (ppm)
Number of hydrogens per structure







Vinyl
4.95-5.10
2


Vinylidene
4.70-4.84
2


Vinylene
5.31-5.55
2


Trisubstituted
5.11-5.30
1









The populations of olefin unsaturations found in the products by 1H NMR are summarized in Table 3. In this table, the vinyl population, as a percentage of total unsaturation, is provided as well, along with the number average molecular weight calculated by assuming one unsaturation per chain and degree of polymerization, or average number of propylene units per chain. For the propylene oligomer products, the % vinyl ranges from  ̃0 (comparative examples A and B catalysts) to as high as  ̃98% (F). Regardless of activator, the less sterically encumbered A, B catalysts (comparative examples) did not produce significant vinyl populations, and the metallocenes D, G and H also produce products with low allylic vinyl content (10 to 42%). In the case of E, the activator appears to impact the chain termination pathway. In the case of F runs, high allylic vinyl populations were attained with both 1 and 4 activators, although allylic vinyl population decreased modestly with increasing polymerization temperature. Temperature played a role in the % vinyl for E but less so for F. Where impact was observed, it was opposite to using bridged, chiral metallocenes.
Glass Transition Temperature (Tg) was measured by DSC as described above.
Viscosity was measured at 35° C. using a Brookfield viscometer.
Refractive Index was measured at 25° C. with 589 nm Na line.
Materials
The following metallocenes were used:

    A=bis(1-methyl,3-n-butylcyclopentadienyl)zirconium dimethyl;
    B=dimethylsilyl bis(4,5,6,7-tetrahydroindenyl)zircomium dimethyl;
    C=dimethylsilyl bis(indenyl)hafnium dimethyl;
    D=(tetramethylcyclopentadienyl)(1,3-dimethylindenyl)zirconium dimethyl;
    E=(tetramethylcyclopentadienyl)(1,3-dimethylindenyl)hafnium dimethyl;
    F=(pentamethylcyclopentadienyl)(1,3-dimethylindenyl)hafnium dimethyl;
    G=(tetramethylcyclopentadienyl)(1-isopropylindenyl)hafnium dimethyl;
    H=(tetramethylcyclopentadienyl)(1-isopropyl,3-n-propylindenyl)hafnium dimethyl; and
    J=dimethylsilyl bis(2-methyl,4-phenylindenyl)zirconium dimethyl.


Several ionic activators and one supported ionic activator were used to activate the metallocenes. The ionic activators used were:

    1=dimethylanilinium perfluorotetraphenylborate,
    2=4-tert-butylanilinium bis(pentafluorophenyl)bis(perfluoro-2-napthyl)borate,
    3=4-tert-butylanilinium (pentafluorophenyl)tris(perfluoro-2-napthyl)borate,
    4=dimethylanilinium tetrakis(perfluoro-2-napthyl)borate,
    5=dimethylanilinium tetrakis(3,5 (pentafluorophenyl)perfluorophenylborate); and
    6=tris-perfluorophenyl boron.


Catalyst Compound Synthesis: Typical dry-box procedures for synthesis of air-sensitive compounds were followed. Solvents were purchased from Aldrich and dried over 2A sieves. Indene was purchased from Aldrich and pentamethylcyclopentadiene was purchased from Norquay. Metallocenes A, B and C were purchased from Boulder scientific or Albemarle. The activators were purchased from Albemarle or Grace Davison.
Catalyst F: (CpMe5)(1,3-Me2C9H5)HfMe2 
LiC9H7 was generated in Et2O (−35° C.) by the reaction of 29 g indene (0.25 mol) with 1 equivalent of n-BuLi (10 M, hexane) added slowly. LiC9H7 was isolated by reduction of the ether solution, addition of hexane and filtration over a medium glass frit. The product was washed with additional hexane (2×40 mL). LiC9H7 was dissolved in Et2O, cooled to −35° C. and reacted with excess MeI (0.375 mol, 47.6 g). After 2 hours the reaction mixture was warmed to ambient temperature. 1-MeC9H7 was isolated as a colorless liquid by aqueous work-up and ether extractions. Similarly 1,3-Me2C9H6 was synthesized by lithiation of MeC9H7, methylation with MeI and aqueous work-up. [Li][1,3-Me2C9H5] was synthesized by reaction of 1,3-Me2C9H6 in hexane with excess nBuLi (1.1 equiv) for 12 hours. The white solid was filtered and washed with additional hexane and dried in vacuo to yield pure [Li][1,3-Me2C9H5], B (14.5 g). 1H NMR (THF-d8, 300 MHz) δ ppm; 7.25-7.10 (m, C6H4, 2H), 6.45-6.30, C6H4, 2H), 6.10 (s, 2-indenyl proton, 1H), 2.35 (s, 1,3Me2C9H5, 6 H).
CpMe5HfCl3 (Crowther, D.; Baenziger, N.; Jordan, R.; J. Journal of the American Chemical Society (1991), 113(4), 1455-1457) (10.4 g) was reacted with [Li][1,3-Me2C9H5] (3.7 g, 24.8 mmol) in Et2O (100 ml) for 12 hours. The yellow product was collected by filtration over a glass frit and dried to yield crude (CpMe5)(1,3-Me2C9H5)HfCl2(8.6 g) as a mixture with LiCl.
1H NMR (CD2Cl2, 300 MHz) δ ppm; 7.58-7.11 (m, C6H4), 6.17 (s, 2-indenyl proton), 2.32 (s, 1,3Me2C9H5), 2.09 (s, CpMe5).
Crude (CpMe5)(1,3-Me2C9H5)HfCl2 (2.5 g) was slurried in toluene (100 ml) and reacted with MeMgI (4.2 g, 2.1 equiv, 3.0 M in Et2O). The reaction mixture was heated to 80° C. for 3 hours. After cooling the volatiles were removed in vacuo to yield a solid which was extracted with hexane (4×40 mL). Hexane was removed from the combined extractions to yield solid yellow (CpMe5)(1,3-Me2C9H5)HfMe2, E (1.6 g). 1H NMR(C6D6, 300 MHz) δ ppm; 7.55-7.48 (m, C6H4, 2H), 7.20-7.16 (m, C9H5, 3H), 2.00 (s, 1,3Me2C9H5, 6H), 1.76 (s, CpMe5, 15H), −0.95 (s, Hf-Me, 6H).
Catalyst D: (CpMe4)(1,3-Me2C9H5)ZrMe2 
ZrCl4 (36 g) was slurried in CH2Cl2 (200 mL) and then reacted with Me2S (19.2 g) for 1 hour. CpMe4HSiMe3 (34 g) was added slowly to the reaction mixture. Yellow solid began to precipitate after several hours and was filtered to yield a first crop of 21.3 g of light yellow solid product. (CpMe4H)ZrCl3.(SMe2)x 1H NMR (CD2Cl2, 300 MHz) δ ppm; 6.05 (s, CpMe4H), 2.6 (br s, MeS), 2.27 (s, CpMe4), 2.20 (s, CpMe4).
(CpMe4H)ZrCl3 (15.0 g) was slurried in Et2O (250 mL) and reacted with [Li][1,3-Me2C9H5] (7.5 g) for 16 hours. The reaction product was filtered over a glass frit, washed with CH2Cl2 and dried in vacuo. All the solid product (ca 22 g) was slurried in Et2O (200 mL) and reacted with MeMgI (38 g 3 M in Et2O). After 4 hours dimethoxyethane (6.8 g) was added and the reaction mixture filtered. Additional Et2O was used to extract the solid residue. The filtrates were reduced and cooled to −35° C. An off-white solid product was filtered and dried in vacuo (14.8 g). (CpMe4)(1,3-Me2C9H5)ZrMe2.
1H NMR (CD2Cl2, 500 MHz) δ ppm; 7.35, 7.05 (m, C9H5), 5.51 (s, C9H5), 4.83 (s, CpMe4H), 2.17 (s, Me2C9H5), 1.79, 1.70 (s, CpMe4H), −1.31 ZrMe.
Catalyst E: (CpMe4)(1,3-Me2C9H5)HfMe2 
HfCl4 (31 g) was slurried in CH2Cl2 (200 mL) and reacted slowly with CpMe4HSiMe3 for several hours. The reaction mixture was filtered, reduced in volume and hexane (80 mL) was added. The filtrate was cooled to −35° C. The off-white product was collected and dried in vacuo. (CpMe4H)HfCl3 (8.0 g) was dissolved in Et2O (150 mL) and reacted with [Li][1,3-Me2C9H5] (2.8 g). After 1 hour the volatiles were removed and the crude reaction mixture extracted with CH2Cl2 (2×60 mL). The filtrate was reduced in vacuo to a light yellow solid product (7.2 g). All (CpMe4)(1,3-Me2C9H5)HfCl2 (7.2 g) was slurried in toluene (200 mL) and reacted with 2 equivalents of MeMgBr (3 M in Et2O). The reaction mixture was heated to 90° C. for 6 hours. The mixture was cooled to room temperature and dimethoxyethane (3 ml) was added. The volatiles were removed, the residue extracted with CH2Cl2 and the filtrates were reduced in vacuo. The product was collected after cooling to −35° C. (2.85 g). (CpMe4)(1,3-Me2C9H5)HfMe2 1H NMR (CD2Cl2, 500 MHz) δ ppm; 7.35, 7.06 (m, C9H5), 5.50 (s, C9H5), 4.89 (s, CpMe4H), 2.18 (s, Me2C9H5), 1.79, 1.76 (s, CpMe4H), −1.49 HfMe.
Catalyst H: (tetramethylcyclopentadienyl)(1-isopropyl,3-propyl-C9H6)HfMe2 
1-isopropyl, 3-propyl-C9H6 was synthesized by reaction of 1-isopropylindenyl lithium with propyl bromide in Et2O. The lithium salt is synthesized from BuLi in Et2O. [Li][1-isopropyl, 3-propyl-C9H5] (2.1 g) was dissolved in Et2O (60 mL) and reacted with (CpMe4H)HfCl3 (4.0 g). MeMgI (2 equivalents) were added to the reaction mixture, 60 ml toluene added and the reaction was heated to 90° C. After 2 hours the reaction was cooled, volatiles removed and the dimethyl product extracted with hexane. The product was obtained as an amber oil (3.8 g). 1H NMR(C6D6, 300 MHz) δ ppm; 7.48 (d), another doublet partially obscured under solvent 7.02 (m), 5.53 (s), 4.72 (s), 3.25 (p), 2.72 (m), 2.31 (m), 2.83, 2.77, 2.74, 2.73 (s), 1.22 (d), 1.07 (d), −0.73(s, Hf-Me), −1.29 (s, Hf-Me).
Catalyst G: (CpMe4)(1-iC3H7—C9H5)HfMe2 
1-Isopropylindenyl lithium (Bradley et al, OM, 2004, 23, 5332) (2.0 g) was slurried in Et2O (100 mL) and reacted with (CpMe4H)HfCl3 (5.0 g) for 12 hours. The solid product was filtered and washed with hexane (3.7 g). (CpMe4)(1-iC3H7—C9H5)HfCl2 1H NMR (C6D6, 300 MHz) δ ppm; 7.55, 7.41 (d), 6.95 (p), 6.22 (d), 5.51 (d), 4.96 (s), 3.72 (p), 1.93, 1.92, 1.83, 1.64 (s), 1.34, 1.11 (d).
The dichloride was slurried in toluene (50 mL) and reacted with 2 equivalents of MeMgI (3 M in Et2O). The reaction was heated to 90° C. for 2 hours and then cooled. The volatiles were removed. The crude mixture was extracted with hexane (2×40 mL), filtered and filtrate reduced to solid product in vacuo (3.1 g). 1H NMR(C6D6, 300 MHz) δ ppm; −0.52, −1.46 Hf-Me.
TEAL-SiO2: SiO2 Davison 948 calcined at 600° C. was slurried in hexane (30 mL) and reacted with Triethylaluminum (10 mL, 1.9 M in toluene) for 12 hours. The solid was filtered and washed with hexane (2×20 mL). After drying in vacuo the yield was 10.75 g TEAL-SiO2.
Catalyst I
TEAL-SiO2 (2.0 g) was slurried in toluene (30 mL) and reacted with Triphenylcarbonium tetrakisperfluorophenyl borate (142 mg, Grace Davison) for 10 minutes. Metallocene E (56 mg) was added as a solution in toluene (5 mL) to the slurry and allowed to react for 12 hours. The supported catalyst was filtered, washed with hexane and dried in vacuo.
Catalyst K
Similar to Catalyst I, Metallocene E was supported as described above except that 3.8 g TEAL-SiO2, 215 mg of ionic activator 1, and 114 mg of metallocene E were used.
Polymerizations
Propylene oligomer batch or continuous polymerizations were carried out for this study using a 2 L stirred autoclave reactor are described in Table 1. Catalyst solutions were prepared in a dry nitrogen purged Vacuum Atmospheres dry box by adding nearly equimolar (typically 1.00:1.05) quantities of metallocene and activator to 4 mL dry toluene in a 10 mL glass vial. The mixture was stirred for several minutes and then transferred to a clean, oven dried catalyst tube. An example of the basic polymerization procedure follows: 2 mL of 25 wt % tri-n-octyl-aluminum (0.037 g Al) in hexanes as scavenger and 100 mL propylene were added to the reactor. Next the reactor was heated to the selected polymerization temperature and catalyst/activator was flushed from the catalyst tube into the reactor with 100 mL propylene. Additional propylene was optionally added for a total of up to 1000 mL. In some cases, hydrogen was also added from a ballast tank (see Table 2A). Hydrogen partial pressure was as high as 50 psig at the start of the run. Polymerization was carried out for 10 to 60 minutes, and then the reactor was cooled, depressurized, and opened. At this point the collected product typically contained some residual monomer. The residual monomer concentration in the product was initially reduced by “weathering.” In many cases the sample was heated in the oven under nitrogen purge or for a short time with applied vacuum. Some of the lowest molecular weight oligomer product may be lost along with the residual monomer. In some cases, residual monomer is still detected in the product in 1H NMR spectras recorded at 30° C. (but is not detected when spectra are recorded at 120° C.). In the Tables below Polig means propylene oligomer, EP means propylene-ethylene oligomer, Tp means polymerization temperature, P-time means polymerization time, Cat means catalyst, Act means activator, DP means degree of polymerization.







TABLE 1







Summary of Propylene Polymerizations























Addi-








P-

tional


Exam-
Pro-


Cat/Act
Tp
time
Yield
C3


ple
duct
Cat
Act
(mg/mg)
(° C.)
(min)
(g)
**


















  1 #
Polig
A
4
30/60 
90
10
25
***


  2 #
Polig
B
4
10/25 
90
7
110
***


  3 #
Polig
A
4
30/60 
140
10
25
***


  4 #
Polig
C
4
10/25 
140
8
160
***


  5 #
Polig
B
4
4/12 
145
7
140
***


  6 #
Polig
B
1
6/15 
152
5
47
***


  7 #
Polig
B
1
6/15 
130
10
30
***


 8
Polig
D
4
 6/13.1
132
10
5.7
***


 9
Polig
E
4
10/25.7
132
10
19
***


10
Polig
E
4
10/25.7
100
12
31.9
100


11
Polig
E
4
10/25.7
80
12
52.5
100


12
Polig
E
4
10/25.7
80
27
142
400


13
Polig
E
4
10/25.7
60
10
65
***


14
Polig
E
4
12/30.8
75
40
242
500


21
Polig
E
1
10/17.9
132
10
17.9
***


22
Polig
E
1
10/17.9
80
12
46.2
100


23
Polig
E
4
10/25.7
80
27
~127
300


24
Polig
D
4
10/31.5
80
10
8.9
150


26
Polig
E
6
10/11.5
80
30
0
***


  25 {circumflex over ( )}
Polig
K(150


80
30
9.8
250




mg)


  28 {circumflex over ( )}
Polig
I(210


60
30
14.9
***




mg)


27
Polig
E
6
10/11.5
132
30
0
***


30
Polig
E
5
10/45.7
80
30
162
450


31
Polig
E
2
10/23.1
80
30
112
350


32
Polig
E
3
10/25.7
80
30
112
250


36
Polig
E
1
10/17.9
45
30
130
***


37
Polig
H
4
10/25 
80
30
13.2
200


38
Polig
F
4
10/25 
80
30
46.2
250


39
Polig
G
4
10/22.7
80
25
70
150


40
Polig
G
4
10/22.7
100
30
55.7
 70


41
Polig
G
4
10/22.7
132
30
16.2
 40


42
Polig
E
4
10/25.7
38
20
~200
***


44
Polig
E
4
10/25 
60
30
~75
***


45
Polig
E
4
10/25 
37
30
~85
***


46
Polig
E
4
10/25 
100
30
36.7
 80


47
Polig
E
4
10/25 
132
30
~10
***


48
Polig
E
1
10/18 
60
30
~110
***


49
Polig
E
1
10/18 
80
30
~70
280


50
Polig
E
4
10/25 
60
180
~200
***


51
Polig
E
1
10/18 
60
120
~220
***





# comparative,


{circumflex over ( )} supported,


** Additional propylene added,


*** Continuous run using continuous propylene feed from day tank






Propylene-ethylene co-oligomerizations, carried out for this study using a 2 L stirred autoclave reactor, are described in Table 2. Catalyst solutions were prepared in a dry nitrogen purged Vacuum Atmospheres dry box by adding nearly equimolar (typically 1.00:1.05) quantities of metallocene and activator to 4 mL dry toluene in a 10 mL glass vial. The mixture was stirred for several minutes and then transferred to a clean, oven dried catalyst tube. An example of the basic polymerization procedure follows: 2 mL of 25 wt % tri-n-octyl-aluminum in hexanes as scavenger and 300 mL propylene were added to the reactor. Next the reactor was heated to appropriate polymerization temperature and catalyst/activator was flushed from the catalyst tube into the reactor with an additional 300 mL propylene. Ethylene was then added continuously throughout the reaction at partial pressures from less than 5 psi up to 220 psi. After a pre-determined reaction time, the reactor was cooled, depressurized, and opened. At this point the collected product typically contained some residual monomer. The residual monomer concentration in the product was initially reduced by “weathering.” In many cases the sample was heated in the oven under nitrogen purge or for a short time with applied vacuum. Some of the lowest molecular weight oligomer product may be lost along with the residual monomer. Note that catalyst productivities are 28 to 678 times higher than the productivities reported by in Macromolecules 2008 41, 559-567.







TABLE 2







Summary of Propylene-Ethylene Copolymerizations















Cata-





Produc-



lyst/
Mole




tivity,


Exam-
Acti-
metal-
Tp,
Psig
Time,
Yield,
g/mmol/


ple
vator
locene a
° C.
C2=
min
g
hr

















33
E/4
2.13E−05
65
20
10
320
90,122


35
E/4
4.26E−06
60
40
20
127
89,526


52
F/4
8.26E−06
60
40
20
240
87,297


53
F/4
8.26E−06
65
30
10
128
92,838


54
F/4
4.13E−06
60
20
10
178
258,206


55
F/1
2.06E−06
58
<5
30
95
92,055


56
F/1
2.06E−06
70
<5
30
87
84,303


57
F/1
6.19E−06
70
10
60
80
12,920


58
F/1
8.26E−06
68
30
10
158
114,597


59
F/1
4.13E−06
65
50
10
95
137,806


60
F/1
2.07E−06
55
220
10
108
313,329


61
F/1
4.15E−06
65
50
5
46
133,455





a in all cases, slight molar excess (~5-10 mole %) of activator used with metallocene.













TABLE 2A







Propylene Polymerizations with Catalyst


F in the Presence of Hydrogen
















Cat/Activator
H2,
Tp.
Time
Yield
Productivity


Ex
Act
(mg/mg)
psi
(C)
(min)
(g)
g/mmol/hr

















62
4
10/25
7
80
10
342
39768


63
4
  5/12.5
7
27
60
348
13489


64
4
 4/10
7
60
30
225
21803


65
4
 4.5/11.25
7
40
45
428
24579


66
1
5/9
7
29
50
525
33915


67
1
 2/3.5
7
60
60
165
22841


68
1
  6/10.4
7
45
30
487
45375


69
1
 2/3.5
7
40
10
1.5
2180


70
1
 2/3.5
50
40
5
2.3
6689


71
1
4/7
7
50
10
140
101740


72
1
4/7
22
45
10
202
146770


73
1
4/7
50
42
5
30
43622


74
1
4/7
50
47
30
325
78731
















TABLE 3







Characterization Data for Propylene Oligomers













Exam-
%


Tg
Viscosity at
Refractive


ple
Vinyls*
DP*
Mn*
(° C.)
35° C. (cps)
Index
















1
3.35
12.55
526.91





2
5.5
107.5
4516


3
1.50
6.57
275.92


4
28.7
86.1
3618


5
12.6
24.2
1017


6
1.94
6.54
274.51


7
1.64
6.93
291.18


8
14.19
8.23
345.51


9
25.03
4.34
182.43


1.4240


10
41.47
6.89
289.26

3.5


11
57.17
8.95
375.94


12
55.74
9.01
378.28

16.0


13
73.30
26.97
1132.69
−37.3


14
69.63
14.40
604.75


21
30.75
3.54
148.48


22
54.24
7.80
327.72

37.3
1.4489


23
60.88
8.46
355.15


1.4534


24
24.72
46.04
1933.70
−56.9


25
54.11
9.05
379.92


28
63.3
17.48
734.1


29
16.1
45.8
1923


30
55.52
8.52
357.69


31
57.49
8.54
358.70


32
60.45
9.33
391.83


36
62.37
68.17
2862.99
−16.7


37
10.68
8.07
338.90


38
97.20
4.62
194.04


1.4252


39
42.16
7.61
319.42


40
27.06
4.68
196.63


1.4298


41
15.14
3.59
150.81


42
74.12
106.5
4472.84


44
97.48
7.12
299.02


45
97.61
24.12
1013.02


46
95.02
4.31
181.21


1.4367


47
88.73
3.79
159.25


48
97.49
8.52
357.87


49
97.85
4.68
196.41


1.4205


50
96.24
8.14
341.96


51
97.13
8.24
346.28


1.4422


62
97.1
6.31
265


63
96.5
22.49
945


64
96.7
6.55
275


65
98.2
13.59
570


66
97.2
19.97
838


67
98.0
6.21
261


68
97.4
10.31
433


71
98.0
6.79
285.4


72
98.2
7.52
315.7


73
96.7
10.56
443.5


74
97.4
9.07
380.8





% Vinyls = % allyl chain ends,


*1H NMR,


IBCE = isobutyl chain end.













TABLE 3A







GPC-DRI(PP standard)










1H NMR
GPC-DRI (PP Std)












Ex.
H2, psi
MN
MN
MW
MZ















2
0
4516
3245
9600
21306


4
0
3617
3262
9584
22496


5
0
1017
576
2745
12604


13
0
1133
811
7546
675,306


24
0
1934
360
12,359
614,945


33
0
1283
947
3,703
10,279


35
0
4546
4,080
19,065
313,648


36
0
2863
2,075
13,793
1,541,001


42
0
4473
3,410
26,362
180,129


45
0
1013.02
504
2,409
9,196


63
0
945
468
1,736
4,143


64
7
275
106
265
611


65
7
570
255
850
1,883


66
7
838
389
1,810
4,557


67
7
261
98
198
431


68
7
433
183
538
1,142


71
7
285.4
134
395
1,676


72
50
315.7
153
443
1,600


73
7
443.5
102
288
1,143


74
22
380.8
156
564
1,440


52
0
773
378
2,277
22,624


53
0
929
466
9,804
53,617


54
0
795
315
3,577
38,176


55
0
974
651
3,290
23,906


56
0
490
294
1,292
9,395


57
0
112
490
5,208
31,162


58
0
1071
501
6,709
65,024


59
0
1580
633
11,053
118,559


60
0
4861
3,519
71,123
433,478


61
0
1877
900
16,764
348,185
















TABLE 4







Properties of Propylene-Ethylene Copolymers














Mole fraction
Wt fraction






Sam-
propylene in
propylene in
Tg
%


ple
product*
product*
(° C.)
vinyls*
DP*
Mn*
















33
—
—
−45.6
82.5
30.6
1283


35
0.555
0.652
−53.1
84.1
108.2
4545


52
0.629
0.718
−88
95.9
18.4
773


53
0.447
0.578

97.2
22.1
929


54
0.501
0.606

96.4
18.9
795


55
0.428
0.529
−83
95.9
23.2
974


56
0.611
0.702

94.6
11.7
490


57
0.434
0.535

94.9
26.8
1124


58
0.378
0.472

94.8
25.5
1071


59
0.351
0.447

96.5
37.6
1580


60
0.124
0.176

76.4
115.7
4861


61
0.247
0.329

99.1
44.7
1877





*Calculated from 1H NMR % Vinyls = % allyl chain ends






Examples 35 and 52-61 were characterized by 13C NMR as described above then compared to the data in Macromolecules 2008 41, 559-567.







TABLE 5







Allyl chain ends in Propylene-Ethylene Co-oligomers










Source
Wt % ethylene
Mol % ethylene
% allyl chain ends













M-Tab 1†
0.0
0.00
100


M-Tab 1†
21.4
29.0
65.0


M-Tab 1†
29.9
39.0
60.0


M-Tab 1†
51.0
61.0
43.0


Coates Tab 1†
54.2
64.0
42.0


35
34.8
44.5
84.1


52
28.2
37.1
95.9


53
42.2
55.3
97.2


54
39.4
49.9
96.4


55
47.1
57.2
95.9


56
29.8
38.9
94.6


57
46.5
56.6
94.9


58
52.8
62.2
94.8


59
55.3
64.9
96.5


60*
82.4
87.6
76.4*


61
67.1
75.3
99.1





M-Tab is table 1 of † Macromolecules 2008 41, 559-567


*10C exotherm













TABLE 6







percent Chain End Microstructures from 13C NMR











Saturated End
Unsaturated




Groups*
End Groups














Sample
IB-P
IB-E
Vinyl-P
Vinyl-E
Init/Term







52
71.8
28.2
71.7
28.3
1.31



53
64.5
35.5
64.1
35.9
1.32



55
48.6
51.4
61.8
38.2
1.16



56
62.4
37.6
65.6
34.4
1.03










Saturated chain end microstructure analysis reveals the surprising result that propylene is nearly always the first monomer inserted following β-Methyl elimination or transfer involving a growing chain and/or incoming monomer, even in polymers containing up to 52 mole % ethylene.
All documents described herein are incorporated by reference herein, including any priority documents and/or testing procedures to the extent they are not inconsistent with this text. As is apparent from the foregoing general description and the specific embodiments, while forms of the invention have been illustrated and described, various modifications can be made without departing from the spirit and scope of the invention. Accordingly, it is not intended that the invention be limited thereby. Likewise, the term “comprising” is considered synonymous with the term “including” for purposes of Australian law.

## Claims

1. A homogenous process for making a propylene co-oligomer, said process having productivity of at least 4500 g/mmol/hr, wherein the process comprises:
contacting, at a temperature of from 35° C. to 150° C., propylene, 0.1 to 70 mol % ethylene and from 0 to about 5 wt % hydrogen in the presence of a catalyst system comprising an activator and at least one metallocene compound represented by at least one of the formulae:
where:




Hf is hafnium;
each X is, independently, selected from the group consisting of hydrocarbyl radicals having from 1 to 20 carbon atoms, hydrides, amides, alkoxides, sulfides, phosphides, halogens, dienes, amines, phosphines, ethers, and a combination thereof, (two X's may form a part of a fused ring or a ring system;
each Q is, independently carbon or a heteroatom;
each R1 is, independently, a C1 to C8 alkyl group, R1 may the same or different as R2;
each R2 is, independently, a C1 to C8 alkyl group;
each R3 is, independently, hydrogen, or a substituted or unsubstituted hydrocarbyl group having from 1 to 8 carbon atoms, provided that at least three R3 groups are not hydrogen;
each R4 is, independently, hydrogen or a substituted or unsubstituted hydrocarbyl group, a heteroatom or heteroatom containing group;
R5 is hydrogen or a C1 to C8 alkyl group;
R6 is hydrogen or a C1 to C8 alkyl group;
each R7 is, independently, hydrogen, or a C1 to C8 alkyl group, provided that at least seven R7 groups are not hydrogen;
T is a bridge;
each Ra, is independently, hydrogen, halogen or a C1 to C20 hydrocarbyl, and two Ra can form a cyclic structure including aromatic, partially saturated, or saturated cyclic or fused ring system;
and further provided that any two adjacent R groups may form a fused ring or multicenter fused ring system where the rings may be aromatic, partially saturated or saturated.

2. The process of claim 1, wherein the propylene co-oligomer obtained is a co-oligomer having an Mn of 300 to 30,000 g/mol (measured by 1H NMR) comprising 10 to 90 mol % propylene and 10 to 90 mol % of ethylene, wherein the oligomer has at least X % allyl chain ends (relative to total unsaturations), where: 1) X =(−0.94*(mole % ethylene incorporated)+100), when 10 to 60 mole % ethylene is present in the co-oligomer, and 2) X=45, when greater than 60 and less than 70 mole % ethylene is present in the co-oligomer, and 3) X=(1.83*(mole % ethylene incorporated)−83), when 70 to 90 mole % ethylene is present in the co-oligomer.

3. The process of claim 2, wherein the propylene co-oligomer has more than 90% allyl chain ends (relative to total unsaturations).

4. The process of claim 2, wherein the propylene co-oligomer comprises from 85 to 15 mol % ethylene and has more than 80% allyl chain ends (relative to total unsaturations).

5. The process of claim 2, wherein the propylene co-oligomer comprises from 20 to 80 mol % ethylene and has more than 70% allyl chain ends (relative to total unsaturations).

6. The process of claim 2, wherein the propylene co-oligomer comprises from 25 to 70 mol % ethylene and has more than 90% allyl chain ends (relative to total unsaturations).

7. The process of claim 2, wherein the propylene co-oligomer is a liquid at 25° C.

8. The process of claim 2, wherein the Mn is about 500 to about 7,500 g/mol, the Mw is 1,000 to about 20,000 g/mol, and the Mz is about 1400 to about 150,000 g/mol.

9. The process of claim 1, wherein the propylene co-oligomer obtained is a propylene co-oligomer comprising more than 90 mol % propylene and less than 10 mol % ethylene wherein the co-oligomer has: at least 93% allyl chain ends, a number average molecular weight (Mn) of about 500 to about 20,000 g/mol, an isobutyl chain end to allylic vinyl group ratio of 0.8:1 to 1.35:1.0, and less than 100 ppm aluminum.

10. The process of claim 9, wherein the propylene co-oligomer is a liquid at 25° C.

11. The process of claim 1, wherein the propylene co-oligomer obtained is a propylene co-oligomer comprising: at least 50 mol % propylene and from 10 to 50 mol % ethylene, wherein the co-oligomer has: at least 90% allyl chain ends, an Mn of about 150 to about 10,000 g/mol, and an isobutyl chain end to allylic vinyl group ratio of 0.8:1 to 1.2:1.0, wherein monomers having four or more carbon atoms are present at from 0 to 3 mol %.

12. The process of claim 1, wherein the propylene co-oligomer obtained is a propylene co-oligomer comprising: at least 50 mol % propylene, from 0.1 to 45 mol % ethylene, and from 0.1 to 5 mol % C4 to C12 olefin, wherein the oligomer has: at least 90% allyl chain ends, an Mn of about 150 to about 10,000 g/mol, and an isobutyl chain end to allylic vinyl group ratio of 0.8:1 to 1.35:1.0.

13. The process of claim 1, wherein the propylene co-oligomer obtained is a propylene co-oligomer comprising: at least 50 mol % propylene, from 0.1 to 45 wt % ethylene, and from 0.1 to 5 mol % diene, wherein the oligomer has: at least 90% allyl chain ends, an Mn of about 150 to about 10,000 g/mol, and an isobutyl chain end to allylic vinyl group ratio of 0.7:1 to 1.35:1.0.

14. The process of claim 1, wherein the activator comprises one or more non-coordinating anions.

15. The process of claim 1, wherein the catalyst system comprises one or more of (pentamethylcyclopentadienyl)(1,3 dimethylindenyl) hafnium dimethyl, and (pentamethylcyclopentadienyl)(1,3 dimethylindenyl) hafnium) dichloride.

16. The process of claim 1, wherein the catalyst system comprises one or more of
(1,3-dimethylindenyl)(pentamethylcyclopentadienyl) hafnium dimethyl,
(1,3,4,7-tetramethylindenyl)(pentamethylcyclopentadienyl) hafnium dimethyl,
(1,3-dimethylindenyl)(tetramethylcyclopentadienyl) hafnium dimethyl,
(1,3-diethylindenyl)(pentamethylcyclopentadienyl) hafnium dimethyl,
(1,3-dipropylindenyl)(pentamethylcyclopentadienyl) hafnium dimethyl,
(1-methyl,3-propyllindenyl)(pentamethylcyclopentadienyl) hafnium dimethyl,
(1,3-dimethylindenyl)(tetramethylpropylcyclopentadienyl) hafnium dimethyl,
(1,2,3-trimethylindenyl)(pentamethylcyclopentadienyl) hafnium dimethyl,
(1,3-dimethylbenzindenyl)(pentamethylcyclopentadienyl) hafnium dimethyl,
(9-methylfluorenyl)(pentamethylcyclopentadienyl) hafnium dimethyl,
μ-dihydrosilyl(bis-tetramethylcyclopentadienyl) hafnium dimethyl,
μ-dimethylsilyl(tetramethylcyclopentadienyl)(3-propyltrimethylcyclopentadienyl) hafnium dimethyl,
μ-dicyclopropylsilyl(bis-tetramethylcyclopentadienyl) hafnium dimethyl,
(1,3-dimethylindenyl)(pentamethylcyclopentadienyl) hafnium dihalide,
(1,3,4,7-tetramethylindenyl)(pentamethylcyclopentadienyl) hafnium dihalide,
(1,3-dimethylindenyl)(tetramethylcyclopentadienyl) hafnium dihalide,
(1,3-diethylindenyl)(pentamethylcyclopentadienyl) hafnium dihalide,
(1,3-dipropylindenyl)(pentamethylcyclopentadienyl) hafnium dihalide,
(1-methyl,3-propyllindenyl)(pentamethylcyclopentadienyl) hafnium dihalide,
(1,3-dimethylindenyl)(tetramethylpropylcyclopentadienyl) hafnium dihalide,
(1,2,3-trimethylindenyl)(pentamethylcyclopentadienyl) hafnium dihalide,
(1,3-dimethylbenzindenyl)(pentamethylcyclopentadienyl) hafnium dihalide,
(9-methylfluorenyl)(pentamethylcyclopentadienyl) hafnium dihalide,
μ-dihydrosilyl(bis-tetramethylcyclopentadienyl) hafnium dihalide,
μ-dihydrosilyl(bis-tetramethylcyclopentadienyl) hafnium dihalide,
μ-dimethylsilyl(tetramethylcyclopentadienyl)(3-propyltrimethylcyclopentadienyl) hafnium dihalide, and
μ-dicyclopropylsilyl(bis-tetramethylcyclopentadienyl) hafnium dihalide.

17. The process of claim 1, further comprising functionalizing the propylene co-oligomer.

18. The process of claim 1, further comprising functionalizing the propylene co-oligomer with succinic acid, maleic acid, maleic anhydride or combinations thereof.

19. The process of claim 1, wherein the propylene co-oligomer has an isobutyl chain end to allylic chain end ratio of 0.9:1 to 1.1:1.0.

20. The process of claim 1, wherein the propylene co-oligomer has an Mw/Mn by GPC-DRI of 1.5 to 20 and an isobutyl chain end to allylic vinyl group ratio of 0.8:1 to 1.35:1.0.

21. The process of claim 1, wherein the Mw/Mn is 1.7 to 10.

22. The process of claim 1, wherein the propylene co-oligomer has a number average molecular weight (Mn) of about 600 to about 15,000 g/mol.

23. The process of claim 1, wherein X is 95%.

24. The process of claim 1, wherein the propylene co-oligomer has an Mn of about 400 to about 10,000 g/mol.

25. The process of claim 1, wherein the propylene co-oligomer has an Mn of 300 to 30,000 g/mol (measured by 1H NMR) and comprises 10 to 50 mol % propylene and 50 to 90 mol % of ethylene, wherein the propylene co-oligomer has at least X % allyl chain ends (relative to total unsaturations), where: 1) X=(1.20(−0.94*(mole % ethylene incorporated)+100)), when 50 to 60 mole % ethylene is present in the propylene co-oligomer, and 2) X=50, when greater than 60 and less than 70 mole % ethylene is present in the propylene co-oligomer, and 3) X=(1.20(1.83*(mole % ethylene incorporated) −83)), when 70 to 90 mole % ethylene is present in the prop co-oligomer.

26. The process of claim 1, wherein the propylene co-oligomer has an Mn of 300 to 30,000 g/mol (measured by 1H NMR) and comprises 10 to 50 mol % propylene and 50 to 90 mol % of ethylene, wherein the propylene co-oligomer has at least X % allyl chain ends (relative to total unsaturations), where: 1) X=(1.50(−0.94*(mole % ethylene incorporated)+100)), when 50 to 60 mole % ethylene is present in the propylene co-oligomer, and 2) X=60, when greater than 60 and less than 70 mole % ethylene is present in the propylene co-oligomer, and 3) X=(1.50(1.83*(mole % ethylene incorporated)−83)), when 70 to 90 mole % ethylene is present in the propylene co-oligomer.

27. The process of claim 1, wherein the propylene co-oligomer has at least 80% isobutyl chain ends.

28. The process of claim 1, wherein the propylene co-oligomer has an isobutyl chain end to allylic chain end ratio of 0.8:1 to 1.35:1.0.

29. The process of claim 1, wherein the propylene co-oligomer has an isobutyl chain end to allylic chain end ratio of 0.9:1 to 1.2:1.0.

30. The process of claim 1, wherein the propylene co-oligomer has been functionalized by reacting a heteroatom containing group with the propylene co-oligomer, with or without catalyst.

31. The process of claim 30, wherein the heteroatom containing group is an amine, an aldehyde, an alcohol, or an acid.

32. The process of claim 30, wherein the heteroatom containing group is succinic acid, maleic acid or maleic anhydride.

33. The process of claim 1, wherein the propylene co-oligomer has a Tg of 0° C. or less.

34. The process of claim 1, wherein the propylene co-oligomer has a melting point of from 60 to 130° C.

35. The process of claim 1, wherein the propylene co-oligomer has no dectectable melting point by DSC following storage at 23° C. for 48 hours.

36. A homogenous process for making a propylene homo-oligomer, said process having productivity of at least 4500 g/mmol/hour, wherein the process comprises:
contacting, at a temperature of from 30° C. to 120° C., propylene, 0 mol % comonomer and from 0 to about 5 wt % hydrogen in the presence of a catalyst system comprising an activator and at least one metallocene compound represented by the formulae:
where




Hf is hafnium;
each X is, independently, selected from the group consisting of hydrocarbyl radicals having from 1 to 20 carbon atoms, hydrides, amides, alkoxides, sulfides, phosphides, halogens, dienes, amines, phosphines, ethers, and a combination thereof, (two X's may form a part of a fused ring or a ring system;
each Q is, independently carbon or a heteroatom;
each R1 is, independently, a C1 to C8 alkyl group, R1 may the same or different as R2;
each R2 is, independently, a C1 to C8 alkyl group;
each R3 is, independently, hydrogen, or a substituted or unsubstituted hydrocarbyl group having from 1 to 8 carbon atoms, provided that: 1) all five R3 groups are methyl, or 2) four R3 groups are not hydrogen and at least one R3 group is a C2 to C8 substituted or unsubstituted hydrocarbyl;
each R4 is, independently, hydrogen or a substituted or unsubstituted hydrocarbyl group, a heteroatom or heteroatom containing group;
R5 is hydrogen or a C1 to C8 alkyl group;
R6 is hydrogen or a C1 to C8 alkyl group;
each R7 is, independently, hydrogen, or a C1 to C8 alkyl group, provided that at least seven R7 groups are not hydrogen;
T is a bridge;
each Ra, is independently, hydrogen, halogen or a C1 to C20 hydrocarbyl, and two Ra can form a cyclic structure including aromatic, partially saturated, or saturated cyclic or fused ring system;
and further provided that any two adjacent R groups may form a fused ring or multicenter fused ring system where the rings may be aromatic, partially saturated or saturated.

37. The process of claim 36, wherein the propylene oligomer obtained is a homo-oligomer, comprising propylene, wherein the homo-oligomer has: at least 93% allyl chain ends, an Mn of about 500 to about 20,000 g/mol, an isobutyl chain end to allylic vinyl group ratio of 0.8:1 to 1.2:1.0, and less than 1400 ppm aluminum.

38. The homo-oligomer of claim 37, wherein the propylene homo-oligomer is a liquid at 25° C.

39. The process of claim 36, wherein the activator comprises one or more non-coordinating anions.

40. The process of claim 36, wherein the catalyst system comprises one or more of
(1,3-dimethylindenyl)(pentamethylcyclopentadienyl) hafnium dimethyl,
(1,3,4,7-tetramethylindenyl)(pentamethylcyclopentadienyl) hafnium dimethyl,
(1,3-diethylindenyl)(pentamethylcyclopentadienyl) hafnium dimethyl,
(1,3-dipropylindenyl)(pentamethylcyclopentadienyl) hafnium dimethyl,
(1-methyl,3-propyllindenyl)(pentamethylcyclopentadienyl) hafnium dimethyl,
(1,2,3-trimethylindenyl)(pentamethylcyclopentadienyl) hafnium dimethyl,
(1,3-dimethylbenzindenyl)(pentamethylcyclopentadienyl) hafnium dimethyl,
(9-methylfluorenyl)(pentamethylcyclopentadienyl) hafnium dimethyl,
(1,3-dimethylindenyl)(pentamethylcyclopentadienyl) hafnium dihalide,
(1,3,4,7-tetramethylindenyl)(pentamethylcyclopentadienyl) hafnium dihalide,
(1,3-diethylindenyl)(pentamethylcyclopentadienyl) hafnium dihalide,
(1,3-dipropylindenyl)(pentamethylcyclopentadienyl) hafnium dihalide,
(1-methyl-3-propyllindenyl)(pentamethylcyclopentadienyl) hafnium dihalide,
(1,2,3-trimethylindenyl)(pentamethylcyclopentadienyl) hafnium dihalide,
(1,3-dimethylbenzindenyl)(pentamethylcyclopentadienyl) hafnium dihalide, and.

41. The process of claim 36, further comprising functionalizing the propylene homo-oligomer.

42. The process of claim 36, wherein the propylene homo-oligomer has a Tg of 0° C. or less.

43. The process of claim 36, wherein the propylene homo-oligomer has a melting point of from 60 to 130° C.

44. The process of claim 36, wherein the propylene homo-oligomer has no detectable melting point by DSC following storage at 23° C. for 48 hours.

45. The process of claim 36, wherein the propylene homo-oligomer comprises propylene and 0 wt % comonomer, and has: at least 95% allyl chain ends, an Mn of about 700 to about 10,000 g/mol, an isobutyl chain end to allylic vinyl group ratio of 0.8:1 to 1.2:1.0, and less than 1400 ppm aluminum.

46. The process of claim 36, wherein the propylene homo-oligomer comprises propylene and 0 wt % comonomer, and has: at least 98% allyl chain ends, an Mn of about 500 to about 20,000 g/mol, an isobutyl chain end to allylic vinyl group ratio of 0.8:1 to 1.2:1.0, and less than 1400 ppm aluminum.

47. The process of claim 36, wherein the propylene homo-oligomer comprises propylene and has: at least 95% allyl chain ends, an Mn of about 500 to about 20,000 g/mol, an isobutyl chain end to allylic vinyl group ratio of 0.8:1 to 1.2:1.0, less than 1400 ppm aluminum, and an Mw/Mn by GPC-DRI of 1.5 to 20.

48. The process of claim 47, wherein the Mw/Mn is 1.7 to 20.

49. The process of claim 47, wherein the Mw/Mn is 1.7 to 10.